Biorefining Method

ABSTRACT

The present invention relates generally to the generation of bio-products from organic matter feedstocks. More specifically, the present invention relates to improved methods for the hydrothermal/thermochemical conversion of lignocellulosic and/or fossilised organic feedstocks into biofuels (e.g. bio-oils) and/or chemical products (e.g. platform chemicals).

INCORPORATION BY CROSS-REFERENCE

This application is a continuation of U.S. patent application Ser. No.16/560,236, filed Sep. 4, 2019, which is a continuation of U.S. patentapplication Ser. No. 14/896,770, filed Dec. 8, 2015, and which issued onOct. 1, 2019 as U.S. Pat. No. 10,427,132, which is the United Statesnational phase of International Application No. PCT/AU2014/000601, filedJun. 11, 2014, which claims priority to Australian provisional patentapplication number 2013902103 filed on Jun. 11, 2013, each of which isincorporated herein by reference in its entirety.

TECHNICAL FIELD

The present invention relates generally to the generation ofbio-products from organic matter feedstocks. More specifically, thepresent invention relates to improved methods for thehydrothermal/thermochemical conversion of lignocellulosic and/orfossilised organic feedstocks into biofuels (e.g. bio-oils) and/orchemical products (e.g. platform chemicals).

BACKGROUND

The global demand for energy continues to rise while reserves ofconventional petroleum (e.g. oil, gas, and natural gas liquids) are indecline. This has led to increased focus and research intounconventional fuel resources (e.g. heavy oil, oil sands, oil shale) andother non-fossil sources of energy (e.g. lignocellulosic materials).

A significant amount of research in the field of “alternative” energyproduction has focussed on the generation of biofuels fromlignocellulosic matter. This technology raises the prospect of a shiftto an abundant and renewable feedstock for energy production as analternative to the depleting reserves of hydrocarbon-based rawmaterials. The enrichment of low energy density fossil fuels (e.g.lignite, peat and oil shale) into high energy fuel products alsorepresents an attractive alternative given the relative abundance ofthose resources.

In particular, the thermochemical conversion of biomass and othercomplex organic matter into biofuels and chemicals based on hydrothermalreactions has shown significant promise. In general, it is desirablethat such methods are continuous or at least semi-continuous in naturewhich may lead to improved product characteristics and/or improvedprocess economics in comparison to batch processes. Process economicsare also more favourable when increased concentrations of organic matterare used in the thermochemical conversion steps, because the amount ofwater or other solvent that must be heated to elevated temperatures isless. However, when high concentrations of organic matter are convertedat elevated temperature and pressure the main products are frequentlyviscous solutions. A common problem in such situations is a partialde-solubilisation of organic and incidental inorganic matter, leading todeposition on apparatus surfaces, otherwise known as “scaling”.Additionally, when water is used as the primary depolymerisation agentswelling of organic matter can occur restricting the concentration thatcan be used. The high levels of energy needed to raise and maintainwater at reaction temperature can also result in charring on the insideof reactor vessel walls. With prolonged operation such deposits can havean adverse effect on the process, necessitating time-consuming andcostly descaling operations in order to restore process performance.Furthermore, at high concentrations of organic matter, the presentinventors have observed that a pressure differential (i.e. a pressuregradient) develops along the length of tube reactors under continuousflow operations which is detrimental to process efficiency.

A need exists for improved methods capable of reducing or avoidingproblems such as scaling, charring and/or the development of pressuregradients across reactors during the thermochemical conversion oforganic matter into bio-products.

SUMMARY OF THE INVENTION

The present inventors have unexpectedly identified that the inclusion ofan effective amount of solid substrate to organic matter feedstock usedin thermochemical conversion processes reduces scaling and/or reducesthe development of pressure differentials during treatment.

In a first aspect, the present invention provides a method for producinga bio-product from organic matter feedstock, the method comprising:

providing a reaction mixture comprising the organic matter feedstock, asolvent, and a solid substrate;

treating the reaction mixture in a reactor vessel at a reactiontemperature and pressure suitable for conversion of all or a portion ofthe organic matter feedstock into a product mixture comprising thebio-product; and

depressurising and cooling the product mixture;

wherein the solid substrate is solid or substantially solid at thereaction temperature and pressure and;

sequesters organic and/or inorganic matter that de-solubilises withinthe reaction mixture or the product mixture; and/or

alters one or more flow characteristics of the reaction mixture and/orthe product mixture in the reactor vessel.

In a second aspect, the present invention provides a method forinhibiting scaling in a reactor vessel during the conversion of organicmatter feedstock into a bio-product, the method comprising:

providing a reaction mixture comprising the organic matter feedstock, asolvent, and a solid substrate;

treating the reaction mixture at a reaction temperature and pressuresuitable for conversion of all or a portion of the organic matterfeedstock into a product mixture comprising the bio-product; and

depressurising and cooling the product mixture;

wherein the solid substrate is solid or substantially solid at thereaction temperature and pressure and;

sequesters organic and/or inorganic matter that de-solubilises withinthe reaction mixture or the product mixture; and/or

alters one or more flow characteristics of the reaction mixture and/orthe product mixture in the reactor vessel.

In one embodiment of the first and second aspects, the treating isperformed under continuous flow conditions.

In a third aspect, the present invention provides a method forinhibiting development of a pressure gradient in a continuous flowreactor vessel during the conversion of organic matter feedstock into abio-product, the method comprising:

providing a reaction mixture comprising the organic matter feedstock, asolvent, and a solid substrate;

treating the reaction mixture at a reaction temperature and pressuresuitable for conversion of all or a portion of the organic matterfeedstock into a product mixture comprising the bio-product; and

depressurising and cooling the product mixture;

wherein the solid substrate is solid or substantially solid at thereaction temperature and pressure and;

sequesters organic and/or inorganic matter that de-solubilises withinthe reaction mixture or the product mixture; and/or alters one or moreflow characteristics of the reaction mixture and/or the product mixturein the reactor vessel.

In one embodiment of the third aspect, the depressurising is facilitatedby a pressure let down device in the reactor vessel;

the reaction mixture is pressurised to a maximum pressure prior to orduring the treating; and

prior to the depressurising facilitated by the pressure let down device,the product mixture is pressurised at less than 98%, less than 95%, lessthan 90%, less than 85%, less than 80%, less than 75%, less than 70%,less than 65%, less than 60%, less than 55%, or less than 50%, of themaximum pressure.

In one embodiment of the first, second or third aspects, the solidsubstrate generates additional metal surface area within the reactorvessel by an abrasive action, to thereby provide additional metalsurface area for provision of additional heterogeneous catalysts to thereaction mixture.

In one embodiment of the first, second or third aspects, the solidsubstrate is inert or substantially inert at the reaction temperatureand pressure.

In one embodiment of the first, second or third aspects, the solidsubstrate is chemically inert or substantially chemically inert at thereaction temperature and pressure.

In one embodiment of the first, second or third aspects, the solidsubstrate is a carbonaceous material comprising at least 50%, at least60%, at least 70%, at least 80%, or at least 90% by weight carbon.

In one embodiment of the first, second or third aspects, the solidsubstrate is selected from the group consisting of: coals, anthraciticcoal, meta-anthracite, anthracite semianthracite, bituminous coal,subbituminous coal, lignite (i.e. brown coal), coking coal, coal tar,coal tar derivatives, coal char, coke, high temperature coke, foundrycoke, low and medium temperature coke, pitch coke, petroleum coke, cokeoven coke, coke breeze, gas coke, brown coal coke, semi coke, charcoal,pyrolysis char, hydrothermal char, carbon black, graphite fineparticles, amorphous carbon, carbon nanotubes, carbon nanofibers,vapor-grown carbon fibers, and any combination thereof.

In one embodiment of the first, second or third aspects, the solidsubstrate is a non-carbonaceous material comprising no more than 10%, nomore than 5%, no more than 1%, or no carbon.

In one embodiment of the first, second or third aspects, the solidsubstrate is selected from the group consisting of fly ash, a mineral,calcium carbonate, calcite, a silicate, silica, quartz, an oxide, ametal oxide, an insoluble or substantially insoluble metal salt, ironore, a clay mineral, talc, gypsum, and any combination thereof.

In another embodiment of the first, second or third aspects, the solidsubstrate is selected from the group consisting of carbonates ofcalcium, carbonates of magnesium, carbonates of calcium and magnesium,calcite, limestone, dolomite, hydroxides of calcium, hydroxides ofmagnesium, oxides of calcium, oxides of magnesium, hydrogen carbonatesof calcium, hydrogen carbonates of magnesium, kaolinite, bentonite,illite, zeolites, calcium phosphate, hydroxyapataite, phyllosilicates,and any combination thereof.

In one embodiment of the first, second or third aspects, the solidsubstrate is provided in the form of a powder, or a slurry comprisingthe powder.

In one embodiment of the first, second or third aspects, the solidsubstrate is present in the reaction mixture at a concentration of morethan 0.5%, more than 1%, more than 3%, more than 5%, more than 10%, morethan 25%, or more than 30% by weight.

In one embodiment of the first, second or third aspects, the solidsubstrate is present in the reaction mixture at a concentration of lessthan 0.5%, less than 1%, less than 3%, less than 5%, less than 10%, lessthan 25%, or less than 50% by weight.

In one embodiment of the first, second or third aspects, thesequestering of the organic and/or inorganic matter by the solidsubstrate comprises adsorbing the organic matter and/or inorganic matteronto a surface of the solid substrate.

In one embodiment of the first, second or third aspects, thesequestering of the organic and/or inorganic matter by the solidsubstrate comprises absorption of the organic matter and/or inorganicmatter into the solid substrate.

In one embodiment of the first, second or third aspects, the organicmatter feedstock is lignocellulosic matter.

In one embodiment of the first, second or third aspects, the organicmatter feedstock is lignocellulosic matter comprising at least 10%lignin, at least 35% cellulose, and at least 20% hemicellulose.

In one embodiment of the first, second or third aspects, the organicmatter feedstock comprises more than about 10% of each of lignin,cellulose, and hemicellulose.

In one embodiment of the first, second or third aspects, the reactionmixture comprises more than 10%, more than 15%, more than 20%, more than30%, more than 35%, or more than 40%, of the organic matter by weight.

In one embodiment of the first, second or third aspects, the reactionmixture comprises less than 10%, less than 15%, less than 20%, less than30%, less than 35%, less than 40%, less than 50%, between 5% and 40%,between 10% to 35%, or between 15% and 30%, of the organic matter byweight.

In one embodiment of the first, second or third aspects, the organicmatter feedstock is provided in the form of a liquid slurry comprisingsome or all of the solvent.

In one embodiment of the first, second or third aspects, the treatingcomprises treating the organic matter, the solid substrate and thesolvent in the form of a slurry.

In one embodiment of the first, second or third aspects, the treating isperformed under conditions of continuous flow and the slurry has a flowvelocity of above 0.01 cm/s, above 0.05 cm/s, above 0.5 cm/s, above 0.1cm/s, above 1.5 cm/s, or above 2.0 cm/s.

In one embodiment of the first, second or third aspects, the methodfurther comprises separating the solid substrate from the productmixture after the depressurising and cooling, and recycling the solidsubstrate into a second slurry or second reaction mixture comprisingorganic matter feedstock.

In one embodiment of the first, second or third aspects, the reactionmixture further comprises an oil additive.

In one embodiment of the first, second or third aspects, the reactionmixture further comprises an oil additive that is mixed with thefeedstock and/or solvent prior to the treating.

In one embodiment of the first, second or third aspects, the reactionmixture further comprises an oil additive that constitutes between 5%and 60%, between 5% and 50%, between 5% and 40%, between 5% and 30%,between 5% and between 20%, more the 5%, more than 10%, more than 15%,more than 20%, more than 30%, less than 20%, less than 15% or less than10% of the oil additive by weight.

In one embodiment of the first, second or third aspects, the reactionmixture further comprises an oil additive selected from the groupconsisting of paraffinic oil, gas-oil, crude oil, synthetic oil,coal-oil, bio-oil, shale oil, kerogen oil, mineral oil, white mineraloil, aromatic oil, tall oil, distilled tall oil, plant or animal oils,fats and their acidic forms and esterified forms, and any combinationthereof.

In one embodiment of the first, second or third aspects, the solvent isa mixed solvent comprising an aqueous solvent component and an oilsolvent component, wherein the two components are substantiallyimmiscible or partly miscible at ambient temperature.

In one embodiment of the first, second or third aspects, the solvent isa mixed solvent comprising an aqueous solvent component and an oilsolvent component, wherein the oil component is crude tall oil,distilled tall oil or a combination thereof.

In one embodiment of the first, second or third aspects, the solventcomprises water and oil in a ratio of about 1:1 by mass, of about 1:2 bymass, of about 2:1 by mass, of about 3:1 by mass, of about 1:3 by mass,of about 1:4 by mass, of about 4:1 by mass, of about 1:5 by mass, ofabout 5:1 by mass, of about 1:6 by mass, of about 6:1 by mass, of about1:7 by mass, of about 7:1 by mass, of about 1:8 by mass, of about 8:1 bymass, of about 1:9 by mass, of about 9:1 by mass, of about 1:10 by mass,or of about 10:1 by mass.

In one embodiment of the first, second or third aspects, the methodfurther comprises separating oil from the product and recycling the oilinto a second slurry or second reaction mixture comprising organicmatter feedstock.

In one embodiment of the first, second or third aspects, the methodfurther comprises separating the solid substrate and oil from theproduct, and recycling the solid substrate and the oil into a secondslurry or second reaction mixture comprising organic matter feedstock.

In one embodiment of the first, second or third aspects, the treatingcomprises treating the reaction mixture at a temperature of between 250°C. and 400° C., and a pressure of between 100 bar and 300 bar.

In one embodiment of the first, second or third aspects, the treatingcomprises treating the reaction mixture at a temperature of between 310°C. and 360° C., and a pressure of between 160 bar and 250 bar.

In one embodiment of the first, second or third aspects, the treatingcomprises treating the reaction mixture at a temperature of between 320°C. and 360° C., and a pressure of between 220 bar and 250 bar.

In one embodiment of the first, second or third aspects, the treatingcomprises treating the reaction mixture at a temperature of between atleast about 100° C., at least about 150° C., at least about 200° C., atleast about 250° C., at least about 300° C., at least about 350° C.,between about 200° C. and about 250° C., between about 200° C. and about400° C., between about 250° C. and about 400° C., between about 250° C.and about 350° C., and between about 250° C. and about 350° C.;generating subcritical or supercritical steam independently of theslurry; and contacting the slurry with the subcritical or supercriticalsteam in at least one vessel or chamber of the reactor vessel.

In one embodiment of the first, second or third aspects, the treatingcomprises pressurising the reaction mixture at a pressure of betweenabout 100 bar and about 400 bar, between about 150 bar and about 400bar, between about 200 bar and about 400 bar, between about 150 bar andabout 350 bar, between about 180 bar and about 350 bar, between about150 bar and about 300 bar, between about 150 bar and about 280 bar,between about 150 bar and about 270 bar, or between about 200 bar andabout 300 bar.

In one embodiment of the first, second or third aspects, the reactionmixture further comprises a catalyst additive.

In one embodiment of the first, second or third aspects, the reactionmixture further comprises a catalyst additive that is mixed with thefeedstock and/or solvent prior to the treating.

In one embodiment of the first, second or third aspects, the catalystadditive is added to the reaction mixture after the reaction mixturereaches said reaction temperature and pressure.

In one embodiment of the first, second or third aspects, the catalystadditive is selected from the group consisting of: a base catalyst, analkali metal hydroxide catalyst, a transition metal hydroxide catalyst,sodium hydroxide, potassium hydroxide, sodium carbonate, potassiumcarbonate, an acid catalyst, a solid acid catalyst, an alkali metalformate catalyst, a transition metal catalyst, a transition metalformate catalyst, a supported transition metal catalyst, a reactivecarboxylic acid catalyst, a transition metal catalyst, a sulphidecatalyst, a noble metal catalyst, a water-gas-shift catalyst, sodiumformate, potassium formate, sodium hydroxide, and combinations thereof.

In one embodiment of the first, second or third aspects, the catalystadditive is not present, or is substantially not present, in any one ormore of the organic matter, the solid substrate, the solvent, or a wallof a reactor vessel in which the method is performed.

In one embodiment of the first, second or third aspects, the catalystadditive is also present in any one or more of the organic matter, thesolid substrate, the solvent, or a wall of a reactor vessel in which themethod is performed.

In one embodiment of the first, second or third aspects, the catalyst isprovided in a slurry comprising the organic matter feedstock, and thecatalyst is between 1% and 30%, between 5% and 30%, between 10% and 30%,between 5% and 30%, between 5% and 20%, between 5% and 15%, between 10%and 30%, between 10% and 30%, between 10% and 15%, less than 20%, lessthan 30%, less than 25%, less than 15%, less than 10%, or less than 5%of the weight of the organic matter in the reaction mixture

In one embodiment of the first, second or third aspects, the reactionmixture comprises the organic matter feedstock (e.g. lignocellulosicmatter) and the solid substrate at a ratio of about 1:1, about 3:2,about 2:1, about 3:1, about 4:1, about 5:1, about 6:1 about 8:1, about10:1, about 20:1, or about 30:1.

In one embodiment of the first, second or third aspects, the solidsubstrate constitutes: at least 1%, at least 2%, at least 3%, at least4%, at least 5%, at least 6%, at least 7%, at least 8%, at least 9%, atleast 10%, at least 15%, at least 20%, at least 30%, at least 40%, atleast 50%, between 1 wt % and 20%, between 1% and 10%, between 1% and5%, between 5% and 10%, between 5% and 15%, between 5% and 20%, between20% and 40%, between 20% and 50%, between 20% and 30%, between 30% and40%, or between 40% and 50% of the total combined mass of the solidsubstrate and organic matter feedstock (e.g. lignocellulosic matter) inthe reaction mixture.

In one embodiment of the first, second or third aspects, the reactionmixture comprises less than 20%, less than 30%, less than 35%, less than40%, less than 40%, less than 70%, less than 80%, less than 90%, lessthan 95%, between 10% and 95%, between 30% and 95%, between 50% to 70%,or between 60% to 80%, of the solvent by weight.

In one embodiment of the first, second or third aspects, the solvent isan aqueous solvent, an oil solvent, or a mixture of an aqueous solventand an oil solvent.

In one embodiment of the first, second or third aspects, the he oilsolvent or the mixture of the aqueous solvent and the oil solventcomprises crude tall oil, distilled tall oil, or a combination thereof.

In one embodiment of the first, second or third aspects, the oil solventis recycled from a bio-product produced according to the method.

In one embodiment of the first, second or third aspects, the solidsubstrate solvent is recycled from a bio-product produced according tothe method.

In one embodiment of the first, second or third aspects, the oil solventand solid substrate are recycled in a mixture from a bio-productproduced according to the method, and the mixture of recycled oil andrecycled substrate is solid at ambient temperature.

In one embodiment of the first, second or third aspects, the aqueoussolvent comprises water, or water and an alcohol.

In one embodiment of the first, second or third aspects, the aqueoussolvent comprises water and an alcohol, and the alcohol is selected fromethanol, methanol, or a combination of methanol and ethanol.

In one embodiment of the first, second or third aspects, prior to and/orafter the treating, the reaction mixture comprises a percentage byweight of said alcohol of more than 3%, more than 5%, more than 10%,more than 15%, more than 20%, more than 25%, more than 30%, less than30%, less than 25%, less than 20%, less than 15%, less than 10%, lessthan 5%, or less than 3%.

In one embodiment of the first, second or third aspects, the bio-productcomprises an oil component having a gross calorific value of at least 30MJ/kg, at least 32 MJ/kg, at least 35 MJ/kg, or at least 36 MJ/kg, and amixed substrate and oil component having a gross calorific value of atleast 26 MJ/kg, at least 28 MJ/kg, at least 30 MJ/kg, at least 32 MJ/kg,or at least 33 MJ/kg.

In one embodiment of the first, second or third aspects, the bio-productcomprises a compound selected from the group consisting of: waxes;aldehydes; carboxylic acids; carbohydrates; phenols; furfurals;alcohols; ketones; resins; resin acids; compounds structurally relatedto resin acids; alkanes; alkenes; fatty acids; fatty acid esters;sterols; sterol-related compounds; furanic oligomers; cyclopentanones;cyclohexanones; alkyl- and alkoxy-cyclopentanones; alkyl- andalkoxy-cyclohexanones; cyclopenteneones; alkyl- andalkoxy-cyclopentenones; aromatic compounds; naphthalenes; alkyl- andalkoxy-substituted naphthalenes; cresols; alkyl- and alkoxy-phenols;alkyl- and alkoxy-catechols; alkyl- and alkoxy-dihydroxybezenes; alkyl-and alkoxy-hydroquinones; indenes; indene-derivatives, and is anycombination thereof.

In one embodiment of the first, second or third aspects, the slurry issubjected to:

(a) heating and pressurisation to a target temperature and pressure,

(b) treatment at target temperature(s) and pressure(s) for a definedtime period (i.e. the “retention time”), and

(c) cooling and de-pressurisation, under continuous flow conditions.

In one embodiment of the first, second or third aspects, the methodcomprises a first preheating stage in which the reaction mixture isheated to a temperature that is below the reaction temperature, and asecond heating stage in which the reaction mixture is heated to thereaction temperature.

In one embodiment of the first, second or third aspects, the secondheating stage comprises contacting the reaction mixture with subcriticalor supercritical steam.

In one embodiment of the first, second or third aspects, the catalystadditive is added to the reaction mixture before the first preheatingstage.

In one embodiment of the first, second or third aspects, the catalystadditive is added to the reaction mixture during or after the firstpreheating stage and prior to the second heating stage.

In one embodiment of the first, second or third aspects, the catalystadditive is added to the reaction mixture during or after the secondheating stage.

In one embodiment of the first, second or third aspects, the treating isfor a time period of between about 20 minutes and about 30 minutes.

In one embodiment of the first, second or third aspects, the methodcomprises the step of heating the organic matter feedstock and solventto the temperature in a time period of less than about 2 minutes, priorto the treating.

In one embodiment of the first, second or third aspects, the methodcomprises the step of heating and pressurising the organic matterfeedstock and solvent to the temperature and pressure in a time periodof less than about 2 minutes, prior to the treating.

In one embodiment of the first, second or third aspects, the methodcomprises the steps of:

(i) cooling the product mixture to a temperature of between about 160°C. and about 200° C. in a time period of less than about 30 secondsafter said treating; and

(ii) depressurisation and cooling the product mixture to ambienttemperature by release through a pressure let down device.

In one embodiment of the first, second or third aspects, the pressurelet down device is enveloped in ambient temperature water.

In one embodiment of the first, second or third aspects, the solidsubstrate is made from residue obtained by distillation or pyrolysis ofthe bio-product.

In one embodiment of the first, second or third aspects, the bio-productcomprises one or more of an oil component, a char component, an aqueouscomponent comprising a solution of organic chemicals in water, and agaseous component comprising: methane, hydrogen, carbon monoxide and/orcarbon dioxide.

In one embodiment of the first, second or third aspects, the bio-productcomprises a bio-oil.

In one embodiment of the first, second or third aspects, the bio-productis fractionated to provide platform chemicals.

In one embodiment of the first, second or third aspects, the treatingcomprises heating and pressurising the slurry in at least one vessel orchamber of the reactor vessel.

In one embodiment of the first, second or third aspects, the treatingcomprises generating subcritical or supercritical steam independently ofthe slurry and contacting the slurry with the subcritical orsupercritical steam in at least one vessel or chamber of said reactorvessel.

In one embodiment of the first, second or third aspects, the slurry isat ambient or near ambient temperature and pressure prior to saidcontacting with the subcritical or supercritical steam.

In one embodiment of the first, second or third aspects, the treatingcomprises: heating the slurry to a temperature selected from the groupconsisting of at least about 100° C., at least about 150° C., at leastabout 200° C., at least about 250° C., at least about 300° C., at leastabout 350° C., between about 200° C. and about 250° C., between about200° C. and about 400° C., between about 250° C. and about 400° C.,between about 250° C. and about 350° C., and between about 250° C. andabout 350° C.; generating subcritical or supercritical steamindependently of the slurry; and contacting the slurry with thesubcritical or supercritical steam in at least one vessel or chamber ofthe reactor vessel.

In one embodiment of the first, second or third aspects, the slurry ispressurised prior to and/or after said contacting.

In one embodiment of the first, second or third aspects, thedepressurising and cooling of the product mixture occurs simultaneously.

In one embodiment of the first, second or third aspects, thedepressurising and cooling of the product mixture occurs separately.

In one embodiment of the first, second or third aspects, the organicmatter feedstock (e.g. lignocellulosic matter) is present in an amountof between 5 wt % and 50 wt %, between 10 wt % and 40 wt %, or between 5wt % and 30 wt %, of the slurry and/or the reaction mixture.

In one embodiment of the first, second or third aspects, the organicmatter feedstock (e.g. lignocellulosic matter) is present in an amountof more than 5 wt % of the slurry and/or the reaction mixture.

In one embodiment of the first, second or third aspects, the organicmatter feedstock (e.g. lignocellulosic matter) is present in an amountof at least 5 wt %, at least 10 wt %, at least 15 wt %, at least 20 wt%, or at least 30 wt % of the slurry and/or the reaction mixture.

In one embodiment of the first, second or third aspects, the solidsubstrate is present in the slurry and/or reaction mixture in an amountof between 0.5 wt % and 50 wt % of the total wt % amount of the organicmatter feedstock (e.g. lignocellulosic matter) present in the slurryand/or reaction mixture.

In one embodiment of the first, second or third aspects, the organicmatter feedstock is wood (e.g. radiat pine).

In a fourth aspect, the present invention provides a bio-productobtained by the method of the first, second or third aspect.

BRIEF DESCRIPTION OF THE DRAWINGS

Preferred embodiments of the present invention will now be described, byway of example only, with reference to the accompanying drawingswherein:

FIG. 1 is a schematic flow diagram showing an apparatus for convertingorganic matter into bio-products in accordance with an embodiment of theinvention. The pressure drop across the reactor is measured betweenpoints 4 and 5.

FIG. 2 is a graph showing measured pressure difference across reactor(pressure in-pressure out) versus experimental duration for experimentswithout (Runs 1-3) and with (Runs 4-9) solid substrate added to reactionmixture containing organic matter.

FIG. 3 is a graph showing TGA curves (weight loss from sample versustemperature) for samples of mixed solid substrate and oil product fromruns 5, 6 and 7. Key: Upper graphs—weight % versus temperature (lefthand axis). Lower graphs—derivative of weight loss w.r.t temperature(right hand axis). Solid line, Run 6. Dashed line ( - - - ) and Dash-dot(_._.) line, Run 5, Dash dot dot (_.._..) line, Run 7.

FIGS. 4A-4E are representative graphs showing gauge pressure near thestart of the reactor (pressure in) and near the end of the reactor(pressure out) versus experimental duration for experiments with andwithout solid substrate added to reaction mixture containing organicmatter. FIG. 4A shows gauge pressure near the start of the reactor(pressure in) and near the end of the reactor (pressure out) versusexperimental duration for a run (Run 1—Table 2) without substrate. FIG.4B shows gauge pressure near the start of the reactor (pressure in) andnear the end of the reactor (pressure out) versus experimental durationfor a run (Run 2—Table 2) without substrate. FIG. 4C shows gaugepressure near the start of the reactor (pressure in) and near the end ofthe reactor (pressure out) versus experimental duration for a run (Run7—Table 2) with substrate (lignite). FIG. 4D shows gauge pressure nearthe start of the reactor (pressure in) and near the end of the reactor(pressure out) versus experimental duration for a run (Run 9—Table 2)with substrate (lignite). FIG. 4E shows gauge pressure near the start ofthe reactor (pressure in) and near the end of the reactor (pressure out)versus experimental duration for a run (Run E—Table 7) with substrate(lignite).

DEFINITIONS

As used in this application, the singular form “a”, “an” and “the”include plural references unless the context clearly dictates otherwise.For example, the term “a catalyst” also includes a plurality ofcatalysts.

As used herein, the term “comprising” means “including.” Variations ofthe word “comprising”, such as “comprise” and “comprises,” havecorrespondingly varied meanings. Thus, for example, a bio-product“comprising” a bio-oil may consist exclusively of bio-oil or may includeother additional substances.

As used herein, the terms “organic matter” and “organic materials” havethe same meaning and encompass any material comprising carbon includingboth fossilised and non-fossilised materials. Non-limiting examples oforganic matter include renewable sources of biomass (e.g.lignocellulosic matter), as well as hydrocarbon-containing materials(e.g. lignite, oil shale and peat) which may be non-renewable.

As used herein the term “bio-product” encompasses any product that canbe obtained by the treatment of organic matter feedstock as definedabove in accordance with the methods of the present invention.Non-limiting examples of bio-products include biofuels (e.g. bio-oils,char products, gaseous products) and chemical products (e.g. platformchemicals, organic acids, furanics, furfural, hydroxymethylfurfural,levoglucosan, sorbitol, cylitol, arabinitol, formaldehyde,acetaldehyde).

As used herein, the term “biofuel” refers to an energy-containingmaterial derived from the treatment of organic matter feedstock asdefined above in accordance with the methods of the present invention.Non-limiting examples of biofuels include bio-oils, char products (e.g.upgraded pulvarised coal injection (PCI) equivalent products and fuelsfor direct injection carbon engines (DICE)), and gaseous products (agaseous product comprising methane, hydrogen, carbon monoxide and/orcarbon dioxide).

As used herein the term “bio-oil” refers to a complex mixture ofcompounds derived from the treatment of organic matter feedstock asdefined above in accordance with the methods of the present invention.The bio-oil may comprise compounds including, but not limited to, anyone or more of alkanes, alkenes, aldehydes, carboxylic acids,carbohydrates, phenols, furfurals, alcohols, and ketones. The bio-oilmay comprise multiple phases including, but not limited to, awater-soluble aqueous phase which may comprise, compounds including, butnot limited to, any one or more of carbohydrates, aldehydes, carboxylicacids, carbohydrates, phenols, furfurals, alcohols, and ketones, resinsand resin acids, and compounds structurally related to resin acids,alkanes and alkenes, fatty acids and fatty acid esters, sterols andsterol-related compounds, furanic oligomers, cyclopentanones, andcyclohexanones, alkyl- and alkoxy-cyclopentanones, and cyclohexanones,cyclopenteneones, alkyl- and alkoxy-cyclopentenones, aromatic compoundsincluding naphthalenes and alkyl- and alkoxy-substituted naphthalenes,cresols, alkyl- and alkoxy-phenols, alkyl- and alkoxy-catechols, alkyl-and alkoxy-dihydroxybezenes, alkyl- and alkoxy-hydroquinones, indenesand indene-derivatives; and a water-insoluble phase which may comprise,compounds including, but not limited to, any one or more of waxes,aldehydes, carboxylic acids, carbohydrates, phenols, furfurals,alcohols, and ketones, resins and resin acids, and compoundsstructurally related to resin acids, alkanes and alkenes, fatty acidsand fatty acid esters, sterols and sterol-related compounds, furanicoligomers, cyclopentanones, and cyclohexanones, alkyl- andalkoxy-cyclopentanones, and cyclohexanones, cyclopenteneones, alkyl- andalkoxy-cyclopentenones, aromatic compounds including naphthalenes andalkyl- and alkoxy-substituted naphthalenes, cresols, alkyl- andalkoxy-phenols, alkyl- and alkoxy-catechols, alkyl- andalkoxy-dihydroxybezenes, alkyl- and alkoxy-hydroquinones, indenes andindene-derivatives.

As used herein, the terms “lignocellulosic matter” and “lignocellulosicbiomass” are used interchangeably and have the same meaning. The termsencompass any substance comprising lignin, cellulose, and hemicellulose.By way of non-limiting example, the lignocellulosic matter may compriseat least 10% lignin, at least 10% cellulose and at least 10%hemicellulose.

As used herein, the term “fossilised organic matter” encompasses anyorganic material that has been subjected to geothermal pressure andtemperature for a period of time sufficient to remove water andconcentrate carbon to significant levels. For example, fossilisedorganic material may comprise more than about 10%, 20%, 30%, 40%, 50%,60%, 70%, 75%, 80%, 85%, 90% or 95 wt % carbon. Non-limiting examples offossilised organic matter include coals (e.g. anthracitic coals such asmeta-anthracite, anthracite and semianthracite; bituminous coals;subbituminous coals; lignite (i.e. brown coal), coking coal, coal tar,coal tar derivatives, coal char), cokes (e.g. high temperature coke,foundry coke, low and medium temperature coke, pitch coke, petroleumcoke, coke oven coke, coke breeze, gas coke, brown coal coke, semicoke), peat (e.g. milled peat, sod peat), kerogen, tar sands, oil shale,shale tar, asphalts, asphaltines, natural bitumen, bituminous sands, orany combination thereof.

As used herein, the term “solvent” includes within its scope an “aqueoussolvent”, an “oil solvent”, and combinations thereof.

As used herein, the term “aqueous solvent” refers to a solventcomprising at least one percent water based on total weight of solvent.An “aqueous solvent” may therefore comprise between one percent waterand one hundred percent water based on total weight of solvent. An“aqueous solvent” will also be understood to include within its scope“aqueous alcohol”, “aqueous ethanol”, and “aqueous methanol”.

As used herein, the term “aqueous alcohol” refers to a solventcomprising at least one percent alcohol based on total weight ofsolvent.

As used herein, the term “aqueous ethanol” refers to a solventcomprising at least one percent ethanol based on total weight ofsolvent.

As used herein, the term “aqueous ethanol” refers to a solventcomprising at least one percent methanol based on total weight ofsolvent.

As used herein, the term “oil solvent” refers to a solvent comprisingany suitable oil, non-limiting examples of which include paraffinic oil,gas-oil, crude oil, synthetic oil, coal-oil, bio-oil, shale oil/kerogenoil, aromatic oils (i.e. single or multi-ringed components or mixturesthereof), tall oils, triglyceride oils, fatty acids, ether extractables,hexane extractables, and any mixture of any of the previous components,and in which the oil constitutes at least one percent of the solventbased on total solvent weight.

As used herein the term “oil additive” refers to any suitable oilcomponent for inclusion in a feedstock, solvent and/or reaction mixtureaccording to the present invention, non-limiting examples of whichinclude paraffinic oil, gas-oil, crude oil, synthetic oil, coal-oil,bio-oil, shale oil/kerogen oil, aromatic oils (i.e. single ormulti-ringed components or mixtures thereof), tall oils, triglycerideoils, fatty acids, ether extractables, hexane extractables, and anymixture of any of the previous components. The oil additive mayconstitute at least one percent portion of the feedstock, solvent and/orreaction mixture to which it is added, based on total weight of thefeedstock, solvent and/or reaction mixture.

As used herein, a “supercritical” substance (e.g. a supercriticalsolvent) refers to a substance that is heated above its criticaltemperature and pressurised above its critical pressure (i.e. asubstance at a temperature and pressure above its critical point).

As used herein, a “subcritical” substance (e.g. a subcritical solvent)refers to a substance at a temperature and/or pressure below thecritical point of the substance. Accordingly, a substance may be“subcritical” at a temperature below its critical point and a pressureabove its critical point, at a temperature above its critical point anda pressure below its critical point, or at a temperature and pressurebelow its critical point.

As used herein, a “solid substrate” is a component that is solid orsubstantially solid at a reaction temperature and pressure used inaccordance with the methods of the present invention. The solidsubstrate may be capable of sequestering organic and/or inorganic matterthat de-solubilises within the reaction mixture and/or a product mixtureproduced from the reaction mixture. Additionally or alternatively, thesolid substrate may be capable of altering the flow characteristics ofthe reaction mixture or the product mixture in a reactor vessel. Solidsubstrates encompass both carbonaceous and non-carbonaceous materials,non-limiting examples of which include coals, anthracitic coal,meta-anthracite, anthracite semianthracite, bituminous coal,subbituminous coal, lignite (i.e. brown coal), coking coal, coal tar,coal tar derivatives, coal char, coke, high temperature coke, foundrycoke, low and medium temperature coke, pitch coke, petroleum coke, cokeoven coke, coke breeze, gas coke, brown coal coke, semi coke, charcoal,pyrolysis char, hydrothermal char, carbon black, graphite fineparticles, amorphous carbon, carbon nanotubes, carbon nanofibers,vapor-grown carbon fibers, fly ash, a mineral, calcium carbonate,calcite, a silicate, silica, quartz, an oxide, a metal oxide, aninsoluble or substantially insoluble metal salt, iron ore, a claymineral, talc, gypsum, carbonates of calcium, carbonates of magnesium,carbonates of calcium and magnesium, calcite, limestone, dolomite,hydroxides of calcium, hydroxides of magnesium, oxides of calcium,oxides of magnesium, hydrogen carbonates of calcium, hydrogen carbonatesof magnesium, kaolinite, bentonite, illite, zeolites, calcium phosphate,hydroxyapataite, phyllosilicates, and any combination thereof.

As used herein, the term “continuous flow” refers to a process wherein aslurry comprising organic matter feedstock and any one or more of: asolvent, solid substrate, catalyst additive and/or oil additive, issubjected to:

(a) heating and pressurisation to a target temperature and pressure,

(b) treatment at target temperature(s) and pressure(s) for a definedtime period (a “retention time”), and

(c) cooling and de-pressurisation;

during which the slurry is maintained in a stream of continuous movementalong the length (or partial length) of a given surface of a reactorvessel. It will be understood that “continuous flow” conditions ascontemplated herein are defined by a starting point of heating andpressurisation (i.e. (a) above) and by an end point of cooling andde-pressurisation (i.e. (c) above). Continuous flow conditions ascontemplated herein imply no particular limitation regarding flowvelocity of the slurry provided that it is maintained in a stream ofcontinuous movement.

As used herein, a “catalyst additive” is a catalyst incorporated into afeedstock slurry and/or reaction mixture that is supplementary tocatalytic compounds intrinsically present in organic matter feedstocktreated in accordance with the methods of the invention, catalyticcompounds intrinsically present in any solvent used in accordance withthe methods of the invention, catalytic compounds intrinsically presentin a solid substrate used to perform the methods of the invention,and/or catalytic compounds intrinsically present in the walls of areactor apparatus used to perform the methods of the invention.

As used herein, the term “intrinsic catalyst” will be understood to be acatalyst that is innately present in a given reaction component such as,for example, any one or more of organic matter feedstock, an aqueoussolvent, and/or vessel walls of a reactor apparatus, or, a catalyst thatform in situ during the treatment process.

As used herein, the terms “reactor”, “reactor apparatus”, and “reactorvessel” are used interchangeably and have the same meaning. Each termencompasses any apparatus suitable for performing the methods of thepresent invention including, for example, continuous flow reactors andbatch reactors.

As used herein a “substantially solid” substrate refers to a substratethat is predominantly solid at a specified reaction temperature and/orpressure in that at least 50%, at least 60%, at least 70%, at least 80%,at least 90%, preferably at least 95%, and more preferably at least 98%of the substrate is in a solid form.

As used herein, a “substantially insoluble” substance is one that ispredominantly insoluble at a specified reaction temperature and/orpressure in that at least 90%, preferably at least 95%, and morepreferably at least 98% of the substrate is not solubilised. As usedherein, an “inert” or “chemically inert” solid substrate is one thatdoes not chemically react with other components in a reaction mixture orcatalyse reactions between components in a reaction mixture, at aspecified reaction temperature and pressure or at a range of reactiontemperatures and pressures.

As used herein, a “substantially inert” or “substantially chemicallyinert” solid substrate one that does not to any significant degreechemically react with other components in a reaction mixture or catalysereactions between components in a reaction mixture, at a specifiedreaction temperature and pressure or at a range of reaction temperaturesand pressures. A “substantially inert” or “substantially chemicallyinert” solid substrate will be understood to react with any othercomponent in a given reaction mixture, or catalyse a reaction betweenany given components in a reaction mixture, on less than 5%, less than4%, less than 3%, less than 2%, or less than 1%, of interaction eventswith the component(s). It will be understood that use of the term“about” herein in reference to a recited numerical value (e.g. atemperature or pressure) includes the recited numerical value andnumerical values within plus or minus ten percent of the recited value.

It will be understood that use of the term “between” herein whenreferring to a range of numerical values encompasses the numericalvalues at each endpoint of the range. For example, a temperature rangeof between 10° C. and 15° C. is inclusive of the temperatures 10° C. and15° C.

Any description of a prior art document herein, or a statement hereinderived from or based on that document, is not an admission that thedocument or derived statement is a part of the common general knowledgeof the relevant art.

For the purposes of description all documents referred to herein areincorporated by reference in their entirety unless otherwise stated.

DETAILED DESCRIPTION OF THE INVENTION

Current methods for the production of bio-oil from organic matter sufferfrom a number of drawbacks. Apart from the generally high oxygen contentand poor stability of most bio-oils, the need to conductdepolymerisation reactions at high temperature and pressure requires areactor apparatus (e.g. continuous flow reactors, batch reactors and thelike) introducing additional difficulties.

For example, water is generally used as the primary depolymerisationagent in hydrothermal liquefaction processes (e.g. hydrothermalupgrading (HTU) and catalytic hydrothermal reactor technology(Cat-HTR)). The use of water restricts the concentration of organicmatter (e.g. lignocellulosic biomass) that can be used in slurryfeedstock in a reactor due to swelling. Moreover, high energy levels arerequired to heat water up to reaction temperature (and maintain itthere) resulting in charring on the inside of the reactor vessel walls.Although the use of a suitable co-solvent such as ethanol offers apotential means of reducing charring it also significantly increases theoverall cost of the process. Ballistic heating is another method thatmay be used to minimise charring. This process involves the rapidconvergence of two separate streams (a slurry stream and asub/supercritical water stream) in a ballistic heating chamber. However,the cost of the supercritical boiler used in ballistic heating andassociated water de-ionisation stage has a significantly adverse effecton cost efficiency.

Another disadvantage of known methods for bio-oil production that usehydrothermal liquefaction of organic matter feedstock is that theproduct typically comprises multiple layers of oil having differentchemical properties. Separation of the different layers can be difficultand requires additional resources.

A further disadvantage of known methods for bio-oil production that usehydrothermal liquefaction of organic matter feedstock is that when highconcentrations of liquefied organic matter (e.g. lignocellulosic matter)are flowing in a tube reactor it has been determined by the presentinventors that a large pressure difference may develop between theupstream and downstream reactor elements. During operation of a largetube reactor under continuous flow conditions a large pressuredifferential is typically sufficient to prevent further operation of thereactor for operational control and safety reasons.

An additional disadvantage of known methods for bio-oil production thatuse hydrothermal liquefaction of organic matter feedstock is that whenhigh concentrations of liquefied organic matter are flowing in a tubereactor it has been observed that organic and/or inorganic matter maydeposit on the reactor walls, particularly where the tube profilechanges, for example at unions or bends linking two straight reactortube elements.

The present invention relates to the unexpected finding that at leastone of the aforementioned disadvantages can be alleviated byincorporating a solid substrate into the feed material and/or reactionmixture used in hydrothermal liquefaction processes. The solid substrateis generally one which remains solid or substantially solid at thereaction temperature and pressure utilised.

Without limitation to particular mechanism(s) of action, it ispostulated that the solid substrate additive may act as an alternativedeposition locus for de-solubilised organic and/or inorganic materialsthat would otherwise deposit as scale on the reactor walls. Thissequestration effect may be enhanced where the substrate has a highsurface area per unit mass. Additionally or alternatively, it isproposed that the presence of the solid substrate may alter the flowcharacteristics of the feedstock slurry, reaction mixture and/or productmixture. These and other potential mechanisms may be responsible for theobserved reduction in pressure differential that otherwise developsbetween the upstream and downstream reactor elements when higherconcentrations of organic matter (e.g. lignocellulosic matter) are usedin slurry feed, and/or the observed reduction in deposition of organicand/or inorganic matter on reactor vessel walls (scaling).

Furthermore and again without limitation to mechanistic theory, it ispostulated that the solid substrate may additionally enhance theproperties of bio-products by the methods of the present invention bymaking available additional metal surface area within the reactor by amild abrasive action on the surfaces that would otherwise be protectedby means of a passivation layer. These additional metal surfaces may actas heterogeneous catalysts for favourable reactions (e.g.decarboxylation and hydrogen-transfer reactions, and other reactiontypes).

Accordingly, certain aspects of the present invention relate to methodsfor producing bio-products by treating organic matter feedstock withvarious solvents and in the presence of solid substrates at increasedtemperature and pressure. Additional aspects of the present inventionrelate to bio-products generated by the methods described herein.

The methods of the present invention are demonstrated to provide severalnotable advantages.

One such advantage is the prevention of pressure build-up and/or scaleformation in reactors during the conversion of organic matter feedstockinto bio-products (e.g. biofuels, platform chemicals) at hightemperature and pressure. In particular, when the conversion process isconducted under continuous flow conditions in a tube reactor or similar,the development of a pressure differential across the reactor and/orscaling on reactor walls may require operations to be terminated andnecessitate expensive and time-consuming de-scaling or cleaningprocedures. A second advantage is that inclusion of the solid substratemay assist in increasing the availability of metal surfaces in thereactor that can partake in heterogeneous catalysis. A third advantageis that if a liquid biofuel is pyrolytically distilled from a productmixture comprising the solid substrate after de-pressurisation andseparation (see methodology in Examples), a char can be generated thatcan be recycled to provide solid substrate for treatment of additionalorganic matter feedstock. Furthermore, char produced in excess of solidsubstrate requirements is a renewable carbon-rich solid product withsuitability for use in bio-char carbon sequestration, fuel and/orchemical applications.

Organic Matter

The present invention provides methods for the conversion of organicmatter feedstock into bio-products (e.g. biofuels including bio-oils;chemical products etc.). As used herein, “organic matter” (also referredto herein as “organic material”) encompasses any matter comprisingcarbon, including both fossilised and non-fossilised forms ofcarbon-comprising matter.

No limitation exists regarding the particular type of organic matterfeedstocks utilised in the methods of the invention, although it iscontemplated that the use of a solid substrate in accordance with themethods of the present invention may be more beneficial during theconversion of non-fossilised forms of organic matter (e.g.lignocellulosic matter) compared to fossilised forms of organic matter.

Organic matter utilised in the methods of the invention may comprisenaturally occurring organic matter (e.g. lignocellulosic biomass and thelike) and/or synthetic organic materials (e.g. synthetic rubbers,plastics, nylons and the like). In some embodiments, organic matterutilised in the methods of the invention comprises a mixture offossilised organic matter and non-fossilised organic matter (e.g.lignocellulosic matter). In such cases, the fossilised organic mattermay remain solid at reaction temperature and pressure in which case itmay act as a solid substrate as described herein. In the case where morethan one type (i.e. a mixture) of organic matter is utilised, nolimitation exists regarding the particular proportion of the differentcomponents of organic matter.

In preferred embodiments, organic matter utilised in the methods of theinvention is or comprises lignocellulosic matter. Lignocellulosic matteras contemplated herein refers to any substance comprising lignin,cellulose and hemicellulose.

For example, the lignocellulosic matter may be a woody plant orcomponent thereof. Examples of suitable woody plants include, but arenot limited to, pine (e.g. Pinus radiata), birch, eucalyptus, bamboo,beech, spruce, fir, cedar, poplar, willow and aspen. The woody plantsmay be coppiced woody plants (e.g. coppiced willow, coppiced aspen).

Additionally or alternatively, the lignocellulosic matter may be afibrous plant or a component thereof. Non-limiting examples of fibrousplants (or components thereof) include grasses (e.g. switchgrass), grassclippings, flax, corn cobs, corn stover, reed, bamboo, bagasse, hemp,sisal, jute, cannibas, hemp, straw, wheat straw, abaca, cotton plant,kenaf, rice hulls, and coconut hair.

Additionally or alternatively, the lignocellulosic matter may be derivedfrom an agricultural source. Non-limiting examples of lignocellulosicmatter from agricultural sources include agricultural crops,agricultural crop residues, and grain processing facility wastes (e.g.wheat/oat hulls, corn fines etc.). In general, lignocellulosic matterfrom agricultural sources may include hard woods, soft woods, hardwoodstems, softwood stems, nut shells, branches, bushes, canes, corn, cornstover, cornhusks, energy crops, forests, fruits, flowers, grains,grasses, herbaceous crops, wheat straw, switchgrass, salix, sugarcanebagasse, cotton seed hairs, leaves, bark, needles, logs, roots,saplings, short rotation woody crops, shrubs, switch grasses, trees,vines, cattle manure, and swine waste.

Additionally or alternatively, the lignocellulosic matter may be derivedfrom commercial or virgin forests (e.g. trees, saplings, forestry ortimber processing residue, scrap wood such as branches, leaves, bark,logs, roots, leaves and products derived from the processing of suchmaterials, waste or byproduct streams from wood products, sawmill andpaper mill discards and off-cuts, sawdust, and particle board).

Additionally or alternatively, the lignocellulosic matter may be derivedfrom industrial products and by-products. Non-limiting examples includewood-related materials and woody wastes and industrial products (e.g.pulp, paper (e.g. newspaper) papermaking sludge, cardboard, textiles andcloths, dextran, and rayon).

It will be understood that organic material used in the methods of theinvention may comprise a mixture of two or more different types oflignocellulosic matter, including any combination of the specificexamples provided above.

The relative proportion of lignin, hemicellulose and cellulose in agiven sample will depend on the specific nature of the lignocellulosicmatter.

By way of example only, the proportion of hemicellulose in a woody orfibrous plant used in the methods of the invention may be between about15% and about 40%, the proportion of cellulose may be between about 30%and about 60%, and the proportion of lignin is may be between about 5%and about 40%. Preferably, the proportion of hemicellulose in the woodyor fibrous plant may be between about 23% and about 32%, the proportionof cellulose may be between about 38% and about 50%, and the proportionof lignin may be between about 15% and about 25%.

In some embodiments, lignocellulosic matter used in the methods of theinvention may comprise between about 2% and about 35% lignin, betweenabout 15% and about 45% cellulose, and between about 10% and about 35%hemicellulose.

In other embodiments, lignocellulosic matter used in the methods of theinvention may comprise between about 20% and about 35% lignin, betweenabout 20% and about 45% cellulose, and between about 20% and about 35%hemicellulose.

In some embodiments, the lignocellulosic matter may comprise more thanabout 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, or 50% lignin.

In some embodiments, the lignocellulosic matter may comprise more thanabout 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, or 50% cellulose.

In some embodiments, the lignocellulosic matter may comprise more thanabout 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, or 50% hemicellulose.

The skilled addressee will recognize that the methods described hereinare not constrained by the relative proportions of lignin, hemicelluloseand cellulose in a given source of lignocellulosic matter.

In certain embodiments of the invention, a mixture of organic materialcomprising lignite (brown coal) and lignocellulosic matter may beutilised as organic matter feedstock in the methods of the invention.The lignocellulosic matter of the mixture may, for example, comprisewoody plant material and/or fibrous plant material. The proportion of slignite in the mixture may be greater than about 20%, 40%, 60% or 80%.Alternatively, the proportion of lignocellulosic matter in the mixturemay be greater than about 20%, 40%, 60% or 80%.

In some preferred embodiments, organic matter utilised in the methods ofthe invention comprises carbon-containing polymeric materials,non-limiting examples of which include rubbers (e.g. tyres), plasticsand polyamides (e.g. nylons).

Non-limiting examples of suitable rubbers include natural and syntheticrubbers such as polyurethanes, styrene rubbers, neoprenes,polybutadiene, fluororubbers, butyl rubbers, silicone rubbers,plantation rubber, acrylate rubbers, thiokols, and nitrile rubbers.

Non-limiting examples of suitable plastics include PVC, polyethylene,polystyrene, terphtalate, polyethylene and polypropylene.

Organic matter feedstocks utilised in the methods of the invention maycomprise carbon-containing wastes such as sewage, manure, or householdor industrial waste materials.

Pre-Treatment of Organic Matter

Organic matter utilised in the methods of the present invention mayoptionally be pre-treated prior converting it into bio-product(s).

It will be recognised that no strict requirement exists to perform apre-treatment step when using the methods described herein. For example,pre-treatment of the organic matter may not be required if it isobtained in the form of a liquid or in a particulate form. However, itis contemplated that in many cases pre-treatment of the organic mattermay be advantageous in enhancing the outcome of the methods describedherein.

In general, pre-treatment may be used to break down the physical and/orchemical structure of the organic matter making it more accessible tovarious reagents utilised in the methods of the invention (e.g.oil-based solvent, catalysts and the like) and/or other reactionparameters (e.g. heat and pressure). In certain embodiments,pre-treatment of organic matter may be performed for the purpose ofincreasing solubility, increasing porosity and/or reducing thecrystallinity of sugar components (e.g. cellulose). Pre-treatment of theorganic matter may be performed using an apparatus such as, for example,an extruder, a pressurized vessel, or batch reactor.

Pre-treatment of the organic matter may comprise physical methods,non-limiting examples of which include grinding, chipping, shredding,milling (e.g. vibratory ball milling), compression/expansion, agitation,and/or pulse-electric field (PEF) treatment.

Additionally or alternatively, pre-treatment of the organic matter maycomprise physio-chemical methods, non-limiting examples of which includepyrolysis, steam explosion, ammonia fiber explosion (AFEX), ammoniarecycle percolation (ARP), and/or carbon-dioxide explosion.Pre-treatment with steam explosion may additionally involve agitation ofthe organic matter.

Additionally or alternatively, pre-treatment of the organic matter maycomprise chemical methods, non-limiting examples of which includeozonolysis, acid hydrolysis (e.g. dilute acid hydrolysis using H₂SO₄and/or HCl), alkaline hydrolysis (e.g. dilute alkaline hydrolysis usingsodium, potassium, calcium and/or ammonium hydroxides), oxidativedelignification (i.e. lignin biodegradation catalysed by the peroxidaseenzyme in the presence of H₂O₂), and/or the organosolvation method (i.e.use of an organic solvent mixture with inorganic acid catalysts such asH₂SO₄ and/or HCl to break lignin-hemicellulose bonds).

Additionally or alternatively, pre-treatment of the organic matter maycomprise biological methods, non-limiting examples of which include theaddition of microorganisms (e.g. rot fungi) capable ofdegrading/decomposing various component(s) of the organic matter.

In some embodiments, organic matter used in the methods of the presentinvention is lignocellulosic matter which may be subjected to anoptional pre-treatment step in which hemicellulose is extracted.Accordingly, the majority of the hemicellulose (or indeed all of thehemicellulose) may be extracted from the lignocellulosic matter and theremaining material (containing predominantly cellulose and lignin) usedto produce a biofuel by the methods of the invention. However, it willbe understood that this pre-treatment is optional and no requirementexists to separate hemicellulose from lignocellulosic matter whenperforming the methods of the present invention. Suitable methods forthe separation of hemicellulose from lignocellulosic matter aredescribed, for example, in PCT publication number WO/2010/034055, theentire contents of which are incorporated herein by reference.

For example, the hemicellulose may be extracted from lignocellulosicmatter by subjecting a slurry comprising the lignocellulosic matter(e.g. 5%-15% w/v solid concentration) to treatment with a mild aqueousacid (e.g. pH 6.5-6.9) at a temperature of between about 100° C. andabout 250° C., a reaction pressure of between about 2 and about 50atmospheres, for between about 5 and about 20 minutes. The solubilisedhemicellulose component may be separated from the remaining solid matter(containing predominantly cellulose and lignin) using any suitable means(e.g. by use of an appropriately sized filter). The remaining solidmatter may be used directly in the methods of the invention, oralternatively mixed with one or more other forms of organic matter (e.g.lignite) for use in the methods of the invention.

Slurry Characteristics

Organic matter feedstock utilised in accordance with the methods of thepresent invention is preferably treated in the form of a slurry. Theslurry may comprise the organic matter in combination with a solvent(e.g. an aqueous solvent, an aqueous alcohol solvent, an aqueous ethanolsolvent, an aqueous methanol solvent) optionally in combination with asolid substrate, a catalyst additive, and/or an oil additive. The slurrymay be generated, for example, by generating a particulate form of theorganic matter (e.g. by physical methods such as those referred to aboveand/or by other means) and mixing with the solvent.

No particular limitation exists regarding the relative proportions ofsolvent, feedstock, oil additive and/or solid substrate in the slurry.Non-limiting examples of potential quantities of these variouscomponents are described in the sections below.

Organic Matter Feedstock Component

A slurry for use in accordance with the methods of the present inventionwill generally comprise organic matter feedstock.

In certain embodiments of the invention, the concentration of organicmatter in the slurry may be less than about 85 wt %, less than about 75wt %, or less than about 50 wt %. Alternatively, the concentration oforganic matter may be more than about 10 wt %, more than about 20 wt %,more than about 30 wt %, more than about 40 wt %, more than about 50 wt%, or more than about 60 wt %. In some embodiments the slurry maycomprise between about 35 wt % and about 45 wt % of an oil additive. Inother embodiments, the slurry may comprise about 40 wt % oil or 39.5 wt% of an oil additive.

The optimal particle size of solid components of the organic matterfeedstock and the optimal concentration of those solids in the slurrymay depend upon factors such as, for example, the heat transfer capacityof the organic matter utilised (i.e. the rate at which heat can betransferred into and through individual particles), the desiredrheological properties of the slurry and/or the compatibility of theslurry with component/s of a given apparatus within which the methods ofthe invention may be performed (e.g. reactor tubing). The optimalparticle size and/or concentration of solid components of the organicmatter components in a slurry used for the methods of the presentinvention can readily be determined by a person skilled in the art usingstandard techniques. For example, a series of slurries may be generated,each sample in the series comprising different particle sizes and/ordifferent concentrations of s the solid organic matter componentscompared to the other samples. Each slurry can then be treated inaccordance with the methods of the invention under a conserved set ofreaction conditions. The optimal particle size and/or concentration ofsolid organic matter components can then be determined upon analysis andcomparison of the products generated from each slurry using standardtechniques in the art.

In certain embodiments of the invention, the particle size of solidorganic matter components in the slurry may be between about 10 micronsand about 10,000 microns. For example, the particle size may be morethan about 50, 100, 500, 750, 1000, 2000, 3000, 4000, 5000, 6000, 7000,8000 or 9000 microns. Alternatively, the particle size may less thanabout 50, 100, 500, 750, 1000, 2000, 3000, 4000, 5000, 6000, 7000, 8000or 9000 microns. In some is embodiments, the particle size is betweenabout 10 microns and about 50 microns, between about 10 microns andabout 100 microns, between about 10 microns and about 200 microns,between about 10 microns and about 500 microns, between about 10 micronsand about 750 microns, or between about 10 microns and about 1000microns. In other embodiments, the particle size is between aboutbetween about 100 microns and about 1000 microns, between about 100microns and about 750 microns, between about 100 microns and about 500microns, or between about 100 microns and about 250 microns.

Solvent Component

A slurry for use in accordance with the methods of the present inventionwill generally comprise a solvent component. The solvent may be anaqueous solvent, an oil solvent, or a combination thereof.

The solvent may comprise or consist of water.

In certain embodiments of the invention, the concentration of water inthe slurry may be above about 80 wt %, above about 85 wt %, or aboveabout 90 wt %. Accordingly, the concentration of water may be aboveabout 75 wt %, above about 70 wt %, above about 60 wt %, above about 50wt %, above about 40 wt %, or above about 30 wt %. In some embodiments,the concentration of water is between about 90 wt % and about 95 wt %.

In some embodiments the slurry comprises between about 10 wt % and about30 wt % water. In other preferred embodiments, the slurry comprisesabout 20 wt % oil or about 15 wt % water.

In some embodiments, the water is recycled from the product of theprocess. For example, a portion water present following completion ofthe reaction may be taken off as a side stream and recycled into theslurry.

The solvent may comprise or consist of one or more aqueous alcohol/s.For example, it may be suitable or preferable to use an aqueous alcoholas the solvent when the organic matter used in the methods consists ofor comprises a significant amount of lignocellulosic material and/orother materials such rubber and plastics due to the stronger chemicalbonds in these types of organic matter.

Suitable alcohols may comprise between one and about ten carbon atoms.Non-limiting examples of suitable alcohols include methanol, ethanol,isopropyl alcohol, isobutyl alcohol, pentyl alcohol, hexanol andiso-hexanol.

The slurry may comprise more than about 5 wt %, 10 wt %, 15 wt %, 20 wt%, 25 wt %, 30 wt %, 35 wt %, 40 wt %, 45 wt % or 50 wt % alcoholaqueous alcohol.

In certain embodiments, the solvent comprises a mixture of two or moreaqueous alcohols. Preferably, the alcohol is ethanol, methanol or amixture thereof.

Solid Substrate Component

A slurry for use in accordance with the methods of the present inventionmay comprise a solid substrate component as described herein.

Favourable characteristics of the solid substrate may include any one ormore of the following: it remains inert or substantially inert at thereaction temperature and pressure used; it remains unaltered orsubstantially unaltered upon completion of the process; it remains as asolid or substantially solid at the reaction temperatures and pressuresused; it is of low or moderate hardness so that it does not inducesubstantial abrasion or erosive corrosion in reactors (e.g. continuousflow reactors); it has a high internal or external specific surface areaso that it can adsorb and/or absorb large quantities of bio-productsand/or other precipitates during the conversion process.

The solid substrate may be a carbonaceous material. By way ofnon-limiting example only, the solid substrate may be a carbonaceousmaterial comprising at least 50%, at least 60%, at least 70%, at least80%, at least 90%, or at least 95% by weight carbon.

Non-limiting examples of suitable carbonaceous materials for use as thesolid substrate include coals (e.g. anthracitic coals such asmeta-anthracite, anthracite and semianthracite; bituminous coals,subbituminous coals, lignite (i.e. brown coal), coking coal, coal tar,coal tar derivatives, coal char); cokes (e.g. high temperature coke,foundry coke, low and medium temperature coke, pitch coke, petroleumcoke, coke oven coke, coke breeze, gas coke, brown coal coke, semicoke); charcoal; pyrolysis char; hydrothermal char; carbon black;graphite fine particles; amorphous carbon; carbon nanotubes; carbonnanofibers; vapor-grown carbon fibers; and any combination thereof.

In some preferred embodiments of the present invention the solidsubstrate may be a carbon rich char made from the previous processing oforganic matter according to the present invention followed by a thermaltreatment in the substantial absence of oxygen to remove volatilematerials (e.g. by pyrolysis or vacuum distillation at temperatures inthe range of 200° C. to 800° C.).

The solid substrate may be a non-carbonaceous material. By way ofnon-limiting example only, the solid substrate may be a non-carbonaceousmaterial comprising less than 20%, less than 10%, less than 5%, lessthan 3%, less than 2%, or less than 1%, by weight carbon, or comprise nocarbon.

Non-limiting examples of suitable non-carbonaceous materials for use asthe solid substrate include ash (e.g. fly ash); minerals (e.g. calciumcarbonate, calcite, silicates, silica, quartz, oxides including ironore, clay minerals, talc, gypsum); an insoluble or substantiallyinsoluble metal salt; and any combination thereof.

Further non-limiting examples of suitable materials for use as the solidsubstrate include carbonates of calcium, carbonates of magnesium,carbonates of calcium and magnesium, calcite, limestone, dolomite,hydroxides of calcium, hydroxides of magnesium, oxides of calcium,oxides of magnesium, hydrogen carbonates of calcium, hydrogen carbonatesof magnesium, kaolinite, bentonite, illite, zeolites, calcium phosphate,hydroxyapataite, phyllosilicates, and any combination thereof.

In certain embodiments of the present invention, the concentration ofsolid substrate in the slurry may be less than about 20 wt %, less thanabout 15 wt %, or less than about 10 wt %. Alternatively, theconcentration of solid substrate may be more than about 0.5 wt %, morethan about 1 wt %, more than about 3 wt %, more than about 5 wt %, morethan about 50 8 wt %, or more than about 10 wt %.

The optimal particle size and optimal concentration of the solidsubstrate may depend upon factors such as, for example, the heattransfer capacity of the organic matter utilised (i.e. the rate at whichheat can be transferred into and through individual particles), thedesired rheological properties of the slurry and/or the compatibility ofthe slurry with component/s of a given apparatus within which themethods of the invention may be performed (e.g. reactor tubing). Theoptimal particle size and/or concentration of the solid substratecomponent in a slurry used for the methods of the invention can readilybe determined by a person skilled in the art using standard techniques.For example, a series of slurries may be generated, each sample in theseries comprising a specific solid substrate of different size and/ordifferent concentration to those of other samples. Each slurry can thenbe treated in accordance with the methods of the invention under aconserved set of reaction conditions. The optimal solid substrate sizeand/or concentration can then be determined upon analysis and comparisonof the products generated from each slurry using standard techniques inthe art.

In certain embodiments of the invention, the size of a solid substratecomponent in the slurry may be between about 10 microns and about 10,000microns. For example, the size may be more than about 50, 100, 500, 750,1000, 2000, 3000, 4000, 5000, 6000, 7000, 8000 or 9000 microns.Alternatively, the size may less than about 50, 100, 500, 750, 1000,2000, 3000, 4000, 5000, 6000, 7000, 8000 or 9000 microns. In someembodiments, the size is between about 10 microns and about 50 microns,between about 10 microns and about 100 microns, between about 10 micronsand about 200 microns, between about 10 microns and about 500 microns,between about 10 microns and about 750 microns, or between about 10microns and about 1000 microns. In other embodiments, the size isbetween about between about 100 microns and about 1000 microns, betweenabout 100 microns and about 750 microns, between about 100 microns andabout 500 microns, or between about 100 microns and about 250 microns.

In some embodiments of the invention, the particle size distributionsand particle surface charge characteristics of the organic mattercomponent of the slurry and/or the solid substrate component of theslurry may be optimized in order to provide desirable slurrycharacteristics when mixed, for example, to obtain minimum viscosity fora given solids content. The optimal particle size and/or particlesurface charge of solid components in a given slurry used can readily bedetermined by a person skilled in the art using standard techniques. Forexample, a series of slurries may be generated, each sample in theseries comprising different particle sizes and/or differentconcentrations of solid components compared to the other samples. Eachslurry can then be treated in accordance with the methods of theinvention under a conserved set of reaction conditions. The optimalparticle size and/or particle surface charge of solid organic mattercomponents can then be determined upon analysis and comparison of theproducts generated from each slurry using standard techniques known inthe art.

Catalysts

The conversion of organic matter feedstock into bio-products using themethods of the present invention may be enhanced by the use of one ormore catalyst additives. Although some catalysts may be an intrinsiccomponent of the organic matter (e.g. minerals), solvent (e.g.hydronium/hydroxide ions of water, compound/s in the oil), solidsubstrate, and/or vessel walls of a reactor apparatus in which theorganic matter may be treated (e.g. transition/noble metals), theinvention contemplates the use of catalyst additive(s) to enhance theproduction of biofuel from organic material.

Accordingly, certain embodiments of the invention relate to theproduction of bio-products from organic matter by treatment with asolvent, a solid substrate and optionally an oil additive underconditions of increased temperature and pressure in the presence of atleast one catalyst additive. By catalyst additive it will be understoodthat the catalyst is is supplementary to catalytic compoundsintrinsically present in the organic matter, solvent, solid substrate,and/or walls of a reactor apparatus in which the method is performed.

For example, an embodiment of the invention in which an organic matterfeedstock (e.g. lignocellulosic matter) is treated with a solvent and asolid substrate under conditions of increased temperature and pressurein a reactor apparatus would not be considered to utilise an catalystadditive.

Alternatively, an embodiment of the invention in which an organic matterfeedstock (e.g. lignocellulosic matter) is mixed with a solvent, a solidsubstrate and a supplementary base catalyst (e.g. sodium hydroxide)added, and the resulting mixture then treated under conditions ofincreased temperature and pressure in a reactor apparatus, the methodwould be considered to utilise an catalyst additive.

Although the use of catalyst additive/s may be advantageous in certaincircumstances, the skilled addressee will recognise that the methods ofthe invention may be performed without using them.

An catalyst additive as contemplated herein may be any catalyst thatenhances the formation of biofuel from organic matter using the methodsof the invention, non-limiting examples of which include base catalysts,acid catalysts, alkali metal hydroxide catalysts, transition metalhydroxide catalysts, alkali metal formate catalysts, transition metalformate catalysts, reactive carboxylic acid catalysts, transition metalcatalysts, sulphide catalysts, noble metal catalysts, water-gas-shiftcatalysts, and combinations thereof. Suitable catalysts are described,for example, in United States of America patent publication number2012-0311658 A1 entitled “Methods for biofuel production”, the entirecontents of which are incorporated herein by reference.

The optimal quantity of an catalyst additive used in the methods of theinvention may depend on a variety of different factors including, forexample, the type of organic matter under treatment, the volume oforganic matter under treatment, the solvent utilised, the specifictemperature and pressure employed during the reaction, the type ofcatalyst and the desired properties of the biofuel product. By followingthe methods of the invention, the optimal quantity of an catalystadditive to be used can be determined by one skilled in the art withoutinventive effort.

In certain embodiments, an catalyst additive or combination of catalystadditives may be used in an amount of between about 0.1% and about 10%w/v catalysts, between about 0.1% and about 7.5% w/v catalysts, betweenabout 0.1% and about 5% w/v is catalysts, between about 0.1% and about2.5% w/v catalysts, between about 0.1% and about 1% w/v catalysts, orbetween about 0.1% and about 0.5% w/v catalysts (in relation to thesolvent).

In general, the catalyst additives may be used to create or assist informing and/or maintaining a reducing environment favouring theconversion of organic matter to biofuel. The reducing environment mayfavour hydrolysis of the organic matter, drive the replacement of oxygenwith hydrogen, and/or stabilise the biofuel formed.

Treatment under subcritical conditions (as opposed to supercriticalconditions) may be advantageous in that less energy is required toperform the methods and reaction components may be better preservedduring treatment. When subcritical conditions are utilised it iscontemplated that the additional use of one or more catalysts may beparticularly beneficial in increasing the yield and/or quality of thebio-products. Further, the cost benefits of reduced input energy (i.e.to maintain subcritical rather than supercritical conditions) andpreservation of the solvent may significantly outweigh the extra costincurred by additionally including one or more of the catalyst additivesdescribed herein.

It is contemplated that under conditions of increased temperature andpressure water molecules in the solvent may dissociate into acidic(hydronium) and basic (hydroxide) ions facilitating hydrolysis of solidorganic matter under treatment (i.e. solid to liquid transformation). Incertain embodiments, the temperature and pressure at which the reactionis performed may be sufficiently high for desired levels of hydrolysisto occur without the use of catalyst additives. In other cases, thetemperature and pressure at which the reaction is performed may not besufficiently high for desired levels of hydrolysis to occur without thefurther addition of catalyst additives.

The catalyst additives may be hydrolysis catalysts. In certainembodiments, the hydrolysis catalysts may be base catalysts. Anysuitable base catalyst may be used.

Non-limiting examples of suitable base catalysts for hydrolysis includealkali metal salts, transition metal salts, organic bases, and mixturesthereof.

The alkali metal salts or transition metal salts may comprise anyinorganic anion(s), non-limiting examples of which include sulfate,sulfite, sulfide, disulfide, phosphate, aluminate, nitrate, nitrite,silicate, hydroxide, methoxide, ethoxide, alkoxide, carbonate and oxide.

Preferred alkali metal or transition metal salts are sodium, potassium,iron, calcium and barium salts, and may comprise one or more anionsselected from phosphate, aluminate, silicate, hydroxide, methoxide,ethoxide, carbonate, sulphate, sulphide, disulphide and oxide.

Non-limiting examples of suitable organic bases include ammonia, basicand polar amino-acids (e.g. lysine, histidine, arginine), benzathin,benzimidazole, betaine, cinchonidine, cinchonine, diethylamine,diisopropylethylamine, ethanolamine, ethylenediamine, imidazole, methylamine, N-methylguanidine, N-methylmorpholine, N-methylpiperidine,phosphazene bases, picoline, piperazine, procain, pyridine, quinidine,quinoline, trialkylamine, tributylamine, triethyl amine, trimethylamineand mixtures thereof.

In certain embodiments, the hydrolysis catalysts may be acid catalystsalthough it will be recognised that acid catalysts may generally slowerin catalysing hydrolysis of the organic matter than base catalysts. Anysuitable acid catalyst may be used.

Non-limiting examples of suitable acid catalysts for hydrolysis includeliquid mineral acids, organic acids, and mixtures thereof. The liquidmineral acids and organic acids may comprise any inorganic anion(s),non-limiting examples of which include aluminate, sulfate, sulfite,sulfide, phosphate, phosphite, nitrate, nitrite, silicate, hydroxide andalkoxide (under supercritical or near supercritical conditions),carbonate and carboxy group anions.

Non-limiting examples of suitable organic acids include acetic acid,butyric acid, caproic acid, citric acid, formic acid, glycolic acid,3-hydroxypropionic acid, lactic acid, oxalic acid propionic acid,succinic acid, uric acid, and mixtures thereof.

In certain embodiments, acid catalyst(s) for hydrolysis may be presentin minerals of the organic matter and/or derived from the in situformation of carboxylic acids and/or phenolics during the treatmentprocess. In these cases the acid catalyst are not catalyst additives,but instead considered to be intrinsic catalysts.

In certain embodiments of the invention, a mixture of one or moreadditive acid hydrolysis catalysts and one or more additive basehydrolysis catalysts may be used to enhance hydrolysis of solid matterunder treatment.

The methods of the invention may employ catalyst additives forhydrolysis of the organic matter (as discussed in the precedingparagraphs). Additionally or alternatively, the methods may utilisecatalysts that increase and/or accelerate the removal of oxygen (eitherdirectly or indirectly) from compounds in the organic matter undertreatment. The removal of oxygen may provide a number of advantageouseffects such as, for example, increasing the energy content andstability of the biofuel produced.

An additive acid catalyst may be used to enhance the removal of oxygen,for example, by dehydration (elimination) of water. Accordingly, incertain embodiments an acid catalyst may be used to enhance hydrolysis,and to enhance the removal of oxygen from organic matter undertreatment.

Any suitable acid catalyst may be used to enhance oxygen removal.Non-limiting examples of suitable acid catalysts for oxygen removalinclude liquid mineral acids, organic acids, and mixtures thereof. Theliquid mineral acids and organic acids may comprise any inorganicanion(s), non-limiting examples of which include aluminate, sulfate,sulfite, sulfide, phosphate, phosphite, nitrate, nitrite, silicate,hydroxide and alkoxide (under supercritical or near supercriticalconditions), carbonate and carboxy group anions.

Non-limiting examples of suitable organic acids include acetic acid,butyric acid, caproic acid, citric acid, formic acid, glycolic acid,3-hydroxypropionic acid, lactic acid, oxalic acid propionic acid,succinic acid, uric acid, and mixtures thereof.

In certain embodiments alumino-silicates including hydrated forms (e.g.zeolites) may be used during the treatment of organic matter to assistin dehydration (elimination) of water.

Additionally or alternatively, the removal of oxygen may be enhanced bythermal means involving decarbonylation of, e.g. aldehydes (giving R₃C—Hand CO gas) and decarboxylation of carboxylic acids in the materialunder treatment (giving R₃C—H and CO₂ gas). The speed of these reactionsmay be enhanced by additive acid and/or transition (noble) metalcatalysts. Any suitable transition or noble metal may be used includingthose supported on solid acids. Non-limiting examples includePt/Al₂O₃/SiO₂, Pd/Al₂O₃/SiO₂, Ni/Al₂O₃/SiO₂, and mixtures thereof.

Additionally or alternatively, a combined acid and hydrogenationcatalyst additive may be used to enhance the removal of oxygen, forexample, by hydrodeoxygenation (i.e. elimination of water (via acidcomponent) and saturation of double bonds (via metal component)). Anysuitable combined acid and hydrogenation catalyst may be used includingthose supported on solid acids. Non-limiting examples includePt/Al₂O₃/SiO₂, Pd/Al₂O₃/SiO₂, Ni/Al₂O₃/SiO₂, NiO/MoO₃, CoO/MoO₃,NiO/WO₂, zeolites loaded with noble metals (e.g. ZSM-5, Beta, ITQ-2),and mixtures thereof.

The methods of the invention may employ catalyst additives that enhancehydrolysis of the organic matter under treatment, and/or catalysts thatenhance the removal of oxygen from compounds in the organic matter (asdiscussed in the preceding paragraphs).

Additionally or alternatively, the methods may utilise catalystadditives that enhance the concentration of hydrogen (either directly orindirectly) into compounds of the organic matter under treatment. Theconcentration of hydrogen may provide a number of advantageous effectssuch as, for example, increasing the energy content and stability of thebiofuel produced.

An additive transfer hydrogenation catalyst may be used to enhance theconcentration of hydrogen into compounds of the organic matter undertreatment, for example, by transfer hydrogenation or in situ hydrogengeneration.

Any suitable transfer hydrogenation catalyst may be used to increase theconcentration of hydrogen. Non-limiting examples of suitable transferhydrogenation catalysts include alkali metal hydroxides (e.g. sodiumhydroxide), transition metal hydroxides, alkali metal formates (e.g.sodium formate), transition metal formates, reactive carboxylic acids,transition or noble metals, and mixtures thereof.

In certain embodiments, an additive sodium hydroxide catalyst isutilised in the reaction mixture at a concentration of between about0.1M and about 0.5M.

In other embodiments additive low-valent iron species catalysts(including their hydrides) are utilised in the reaction mixture,including iron zero homogeneous and heterogeneous species.

The alkali metal hydroxide or formate may comprise any suitable alkalimetal. Preferred alkali metals include sodium, potassium, and mixturesthereof. The transition metal hydroxide or formate may comprise anysuitable transition metal, preferred examples including Fe and Ru. Thereactive carboxylic acid may be any suitable carboxylic acid, preferredexamples including formic acid, acetic acid, and mixtures thereof. Thetransition or noble metal may be any suitable transition or noble metal,preferred examples including platinum, palladium, nickel, ruthenium,rhodium, and mixtures thereof.

Additionally or alternatively, an additive transition metal catalyst maybe used to enhance the concentration of hydrogen into organic matterunder treatment, for example, by hydrogenation with H₂. Non-limitingexamples of suitable transition metal catalysts for hydrogenation withH₂ include zero-valent metals (e.g. iron, platinum, palladium, andnickel), transition metal sulfides (e.g. iron sulfide (FeS,Fe_(x)S_(y)), and mixtures thereof.

Additionally or alternatively, an additive water gas shift catalyst maybe used to enhance the concentration of hydrogen into organic matterunder treatment (i.e. via a water-gas shift reaction). Any suitablewater gas shift (WGS) catalyst may be used including, for example,transition metals, transition metal oxides, and mixtures thereof (e.g.magnetite, platinum-based WGS catalysts, finely divided copper andnickel).

Additionally or alternatively, the concentration of hydrogen intoorganic matter under treatment may be facilitated by in situgasification (i.e. thermal catalysis). The in situ gasification may beenhanced by additive transition metals. Any suitable transition metalmay be used including, for example, those supported on solid acids (e.g.Pt/Al₂O₃/SiO₂, Pd/Al₂O₃/SiO₂, Ni/Al₂O₃/SiO₂, and mixtures thereof), andtransition metal sulfides (e.g. Fe_(x)S_(y), FeS/Al₂O₃, FeS/SiO₂,FeS/Al₂O₃/SiO₂, and mixtures thereof). Table 1 below provides a summaryof various exemplary catalysts that may be employed in the methods ofthe invention and the corresponding reactions that they may catalyse.

TABLE 1 summary catalysts and corresponding reactions Catalyst PreferredCatalyst Family Specific catalysts/ Reaction Type Family Memberexample(s) comments Hydrolysis Base catalysts Sub/super- Hydroxide ioncritical water in sub/super- critical water All alkali and M = anyalkali M = Na, K, Fe, transition metal or transition Ca, Ba salts, bothmetal A = aluminate, cations and A = anions, phosphate, silicate, anionscan including: hydroxide, contribute, aluminate, methoxide, Include allsulfate, sulfite, ethoxide common sulfide carbonate inorganic phosphate,sulphate anions phosphite sulphide Any organic nitrate, nitritedisulphide (FeS₂) base silicate oxide hydroxide alkoxide carbonate oxideammonia, pyridine, etc. Hydrolysis Acid catalysts Sub/super- Hydronium(slower) critical water ion in sub/super- critical water Any liquid HA,where Acids may form mineral or A = anions, from the in-situ organicacid including: formation of aluminate, carboxylic acids, sulfate,sulfite, phenolics and the sulfide presence of phosphate, mineralsphosphite nitrate, nitrite silicate hydroxide alkoxide carbonate carboxygroup Dehydration Acid catalysts Sub/super- Hydronium (elimination)critical water ion in sub/super- critical water Any liquid HA, whereAcids may form mineral or A = anions, from the in-situ organic acidincluding: formation of aluminate, carboxylic acids, sulfate, sulfite,phenolics and the sulfide presence of phosphate, minerals. phosphitezeolites or nitrate, nitrite alumino-silicates silicate in general maybe hydroxide added alkoxide carbonate carboxy group Transfer TransferAll alkali and M = any alkali M = Na, K Hydrogenation or hydrogenationtransition metal or transition A = hydroxide, in-situ H₂ catalystshydroxides and metal formate generation formates A = formic, acetic Allreactive hydroxide, M = Fe, Pd, Pd, carboxylic formate Ni acids Alltransition Ru Rh All transition and noble and noble metals metalsDecarboxylation Largely Acid and All transition Pt/Al₂O3/SiO₂ thermaltransition and noble Pd/Al₂O₃/SiO₂ (noble) metal metals Ni/Al₂O₃/SiO₂cats have been supported on reported to aid solid acids the processDecarbonylation Largely As for As for As for thermal decarboxylationdecarboxylation decarboxylation In-situ gasification Largely Transitionsupported Pt/Al₂O₃/SiO₂ thermal metals transition Pd/Al₂O₃/SiO₂ metalsNi/Al₂O₃/SiO₂ sulfides Fe Fe_(x)S_(y) FeS/Al₂O₃ FeS/SiO₂ FeS/Al₂O₃/SiO₂Water-Gas Shift WGS Standard WGS As per As per literature catalystscatalysts literature Direct Transition Zero valent Fe, Pt, P, Ni asHydrogenation metals metals zero valent with H₂ Sulfides FeS, FexSyHydrode- Combined Transition M = transition Pt/Al₂O₃/SiO₂ oxygenationacid and metal and solid metal Pd/Al₂O₃/SiO₂ hydrogenation acid A =acidic Ni/Al₂O₃/SiO₂ catalyst solid NiO/MoO₃ CoO/MoO₃ NiO/WO₂ zeolitesloaded with noble metals, e.g. ZSM-5, Beta, ITQ-2

Catalyst additives for use in the methods of the invention may beproduced using chemical methods known in the art and/or purchased fromcommercial sources.

It will be understood that no particular limitation exists regarding thetiming at which the catalyst additive(s) may be applied when performingthe methods of the invention. For example, the catalyst additive(s) maybe added to the organic matter, solvent, solid substrate, oil additive,or a mixture of one or more of these components (e.g. a slurry) beforeheating/pressurisation to target reaction temperature and pressure,during heating/pressurisation to target reaction temperature andpressure, and/or after reaction temperature and pressure are reached.The timing of catalyst additive addition may depend on the reactivity ofthe feedstock utilised. For example, highly reactive feedstocks maybenefit from catalyst additive addition close to or at the targetreaction temperature and pressure, whereas less reactive feedstocks mayhave a broader process window for catalyst additive addition (i.e. thecatalysts may be added prior to reaching target reaction temperature andpressure).

Catalyst additives may be included in a reaction mixture used fortreatment according to the present invention prior to heating and/orpressurising the reaction mixture, during heating and/or pressurising ofthe reaction mixture, and/or after the reaction mixture reaches adesired reaction temperature and/or reaction pressure.

Oil Component

In some preferred embodiments of the invention, the slurry, the reactionmixture, or both comprises organic matter mixed with an oil additive.The oil additive may act as an oil-solvent in the reaction. The oil maybe any suitable oil, non-limiting examples of which include paraffinicoil, gas-oil, crude oil, synthetic oil, coal-oil, bio-oil, shaleoil/kerogen oil, aromatic oils (i.e. single or multi-ringed componentsor mixtures thereof), tall oils, triglyceride oils, fatty acids, etherextractables, hexane extractables and any mixture of any of the previouscomponents. The oil may be incorporated into the slurry mixture at anypoint before target reaction temperature and/or pressure are reached.For example, the oil may be added to the slurry in a slurry mixing tankas shown in FIG. 1. Additionally or alternatively, the oil may be addedto the slurry en route to a reactor and/or during heating/pressurisationof the slurry.

In particularly preferred embodiments, the oil is a bio-oil productrecycled from the process. For example, a portion of the bio-oilproduced may be taken off as a side stream and recycled into the slurry,reaction mixture, or both.

In some preferred embodiments, the bio-oil is recycled in combinationwith solid substrate, each being a component of the bio-product. Forexample, a portion of the bio-oil produced mixed with solid substratemay be taken off as a side stream and recycled into the slurry, reactionmixture, or both.

No particular limitation exists regarding the proportion of oil additivein a slurry comprising organic matter treated in accordance with themethods of the present invention. For example, the slurry may comprisemore than about 2 wt % oil, more than about 5 wt % oil, more than about10 wt % oil, or more than about 20, 30, 40, 50, 60 or 70 wt % oil.Alternatively, the slurry may comprise less than about 98 wt % oil, lessthan about 95 wt % oil, less than about 90 wt % oil, or less than about80, 70, 60, 50, 40 or 30 wt % oil.

In some preferred embodiments the slurry comprises between about 10 wt %and about 30 wt % organic matter, between about 2 wt % and about 15 wt %solid substrate, and between about 50 wt % and about 90 wt % solventwhere the solvent is a mixture of oil and aqueous phase in anyproportion.

In some preferred embodiments, the slurry comprises between about 40 wt% and about 50 wt % oil. In other preferred embodiments, the slurrycomprises about 45 wt % oil. In other preferred embodiments the slurrycomprises a feedstock to oil ratio of 0.5-1.2:1. The oil may beparaffinic oil.

Reaction Conditions

In accordance with the methods of the present invention, organic matterfeedstock (e.g. lignocellulosic matter) may be treated with a solvent inthe presence of a solid substrate as described herein, and optionally inthe presence of an oil additive and/or an catalyst additive, underconditions of increased temperature and pressure to producebio-products.

The specific conditions of temperature and pressure used when practicingthe methods of the invention may depend on a number different factorsincluding, for example, the type of solvent used, the type of organicmatter feedstock under treatment, the physical form of the organicmatter feedstock under treatment, the relative proportions of componentsin the reaction mixture (e.g. the proportion of solvent, additive oil,catalyst additives, organic matter feedstock and/or any other additionalcomponent/s), the types of additive catalyst(s) utilised (if present),the retention time, and/or the type of apparatus in which the methodsare performed. These and other factors may be varied in order tooptimise a given set of conditions so as to maximise the yield and/orreduce the processing time. In preferred embodiments, all orsubstantially all of the organic material used as a feedstock isconverted into bio-product(s).

Desired reaction conditions may be achieved, for example, by conductingthe reaction in a suitable apparatus (e.g. a sub/supercritical reactorapparatus) capable of maintaining increased temperature and increasedpressure.

Temperature and Pressure

According to the methods of the present invention a reaction mixture isprovided and treated at a target temperature and pressure for a fixedtime period (“retention time”) facilitating the conversion of organicmatter feedstock (e.g. lignocellulosic matter) into bio-product(s). Thetemperature and/or pressure required to drive conversion of organicfeedstock into biofuel using the methods of the invention will depend ona number of factors including the type of organic matter under treatmentand the relative proportions of components in the reaction (e.g. theproportion of solvent, additive oil, catalyst additives, organic matterfeedstock and/or any other additional component/s), the types ofadditive catalyst(s) utilised (if present), the retention time, and/orthe type of apparatus in which the methods are performed. It will berecognised that various catalyst additives as described herein (seesub-section above entitled “Catalysts”) may be used to increase theefficiency of reactions which may in turn reduce the temperature and/orpressure required to drive conversion of the organic matter tobio-products using a given solvent and a solid substrate. Based on thedescription of the invention provided herein the skilled addressee couldreadily determine appropriate reaction temperature and pressure for agiven reaction mixture. For example, the optimal reaction temperatureand/or pressure for a given feedstock slurry may be readily determinedby the skilled addressee by preparing and running a series of reactionsthat differ only by temperature and/or pressure utilised and analysingthe yield and/or quality of the target bio-product(s) produced.

The skilled addressee will also recognise that the pressure utilised isa function of the slurry components and pressure drop, induced by theslurry, and strongly dependent on any particular reactor design (e.g.pipe diameter and/or length etc).

In certain embodiments, treatment of organic matter feedstock to producea bio-product using the methods of the invention may be conducted attemperature(s) of between about 150° C. and about 550° C. andpressure(s) of between about 10 bar and about 400 bar. Preferably, thereaction mixture is maintained at temperature(s) of between about 150°C. and about 500° C. and pressure(s) of between about 80 bar and about350 bar. More preferably the reaction mixture is maintained attemperature(s) of between about 180° C. and about 400° C. andpressure(s) of between about 100 bar and about 330 bar. Still morepreferably the reaction mixture is maintained at temperature(s) ofbetween about 200° C. and about 380° C. and pressure(s) of between about120 bar and about 250 bar.

In preferred embodiments, the reaction mixture is maintained attemperature(s) of between about 200° C. and about 400° C., andpressure(s) of between about 100 bar and about 300 bar.

In other preferred embodiments, the reaction mixture is maintained attemperature(s) of between about 250° C. and about 380° C., andpressure(s) of between about 50 bar and about 300 bar.

In other preferred embodiments, the reaction mixture is maintained attemperature(s) of between about 320° C. and about 360° C. andpressure(s) of between about 150 bar and about 250 bar. In otherpreferred embodiments, the reaction mixture is maintained attemperature(s) of between about 330° C. and about 350° C. andpressure(s) of between about 230 bar and about 250 bar. In anotherparticularly preferred embodiment, the reaction mixture is maintained attemperature(s) of about 340° C. and pressure(s) of between about 240bar.

In other preferred embodiments, the reaction mixture is maintained attemperature(s) of between about 320° C. and about 360° C., andpressure(s) of between about 220 bar and about 250 bar.

In certain embodiments, the reaction mixture is maintained attemperature(s) of above about 180° C. and pressure(s) above about 150bar. In other embodiments, the reaction mixture is maintained attemperature(s) of above about 200° C. and pressure(s) above about 180bar. In additional embodiments, reaction mixture is maintained attemperature(s) of above about 250° C. and pressure(s) above about 200bar. In other embodiments, reaction mixture is maintained attemperature(s) of above about 300° C. and pressure(s) above about 250bar. In other embodiments, reaction mixture is maintained attemperature(s) of above about 350° C. and pressure(s) above about 300bar.

It will be understood that in certain embodiments a solvent used in themethods of the present invention may be heated and pressurised beyondits critical temperature and/or beyond its critical pressure (i.e.beyond the ‘critical point’ of the solvent). Accordingly, the solventmay be a ‘supercritical’ solvent if heated and pressurised beyond the‘critical point’ of the solvent.

In certain embodiments a solvent used in the methods of the presentinvention may be heated and pressurised to level(s) below its criticaltemperature and pressure (i.e. below the ‘critical point’ of thesolvent). Accordingly, the solvent may be a ‘subcritical’ solvent if itsmaximum temperature and/or maximum pressure is below that of its‘critical point’. Preferably, the ‘subcritical’ solvent is heated and/orpressurised to level(s) approaching the ‘critical point’ of the solvent(e.g. between about 10° C. to about 50° C. below the criticaltemperature and/or between about 10 atmospheres to about 50 atmospheresbelow its critical pressure).

In some embodiments, a solvent used in the methods of the presentinvention may be heated and pressurised to levels both above and belowits critical temperature and pressure (i.e. heated and/or pressurisedboth above and below the ‘critical point’ of the solvent at differenttimes). Accordingly, the solvent may oscillate between ‘subcritical’ and‘supercritical’ states when performing the methods.

Retention Time

The specific time period over which the conversion of organic matterfeedstock may be achieved upon reaching a target temperature andpressure (i.e. the “retention time”) may depend on a number differentfactors including, for example, the type of organic matter undertreatment and the relative proportions of components in the reaction(e.g. the proportion of solvent, additive oil, catalyst additives,organic matter feedstock and/or any other additional component/s), thetypes of additive catalyst(s) utilised (if present), the retention time,and/or the type of apparatus in which the methods are performed. Theseand other factors may be varied in order to optimise a given method soas to maximise the yield and/or reduce the processing time. Preferably,the retention time is sufficient to convert all or substantially all ofthe organic material used as a feedstock into bio-product(s).

In certain embodiments, the retention time is less than about 60minutes, 45 minutes, 30 minutes, 25 minutes, 20 minutes, 15 minutes, 10minutes or less than about 5 minutes. In certain embodiments, theretention time is more than about 60 minutes, 45 minutes, 30 minutes, 25minutes, 20 minutes, 15 minutes, 10 minutes or more than about 5minutes. In other embodiments, the retention time is between about 1minute and about 60 minutes. In additional embodiments, the retentiontime is between about 5 minutes and about 45 minutes, between about 5minutes and about 35 minutes, between about 10 minutes and about 35minutes, or between about 15 minutes and about 30 minutes. In furtherembodiments, the retention time is between about 20 minutes and about 30minutes.

Persons skilled in the art will recognised that various catalystadditives as described herein (see sub-section below entitled“Catalysts”) may be used to increase the efficiency of the treatmentwhich may in turn reduce the retention time required to convert theorganic matter into bio-product(s). Similarly, the retention timerequired will be influenced by the proportions of various components inthe reaction mixture (e.g. water, oil additive, alcohol, solidsubstrates, catalyst additives etc).

The optimal retention time for a given set of reaction conditions asdescribed herein may be readily determined by the skilled addressee bypreparing and running a series of reactions that differ only by theretention time, and analysing the yield and/or quality of bio-product(s)produced.

Heating/Cooling, Pressurisation/De-Pressurisation

A reaction mixture (e.g. in the form of a slurry) comprising organicmatter feedstock (e.g. lignocellulosic matter), solvent, and optionallyone or more catalyst additives as defined herein may be brought to atarget temperature and pressure (i.e. the temperature/pressuremaintained for the “retention time”) over a given time period.

Reaction mixes that do not contain a significant proportion of oiladditive may require a very fast initial conversion to generate somesolvent in-situ. However, the incorporation of oil into the reactionmixture as described herein allows the oil to act as a solvent thusalleviating the requirement for rapid heating/pressurisation.

In some embodiments, the reaction mix undergoes a separate pre-heatingstage prior to reaching reaction temperature. The pre-heating stage maybe performed on a feedstock slurry prior to the full reaction mix beingformed. Alternatively the pre-heating stage may be performed on a slurrycomprising all components of the reaction mixture. In some embodiments,the pre-heating stage raises the temperature of the feedstock slurry orreaction mixture to a maximum temperature of about: 120° C., 130° C.,140° C., 150° C., 160° C., 170° C., 180° C., 190° C., or 200° C. Inother embodiments, the temperature is raised to less than about: 120°C., 130° C., 140° C., 150° C., 160° C., 170° C., 180° C., 190° C., or200° C. In still other embodiments the temperature is raised to betweenabout 100° C. and about 200° C., between about 100° C. and about 180°C., between about 100° C. and about 160° C., between about 120° C. andabout 180° C., or between about 120° C. and about 160° C.

In continuous flow systems, pressure will generally change fromatmospheric to target pressure during the time it takes to cross thepump (i.e. close to instantaneous) whereas in a batch system it willmirror the time that it takes to heat the mixture up.

In some embodiments, the reaction mixture may be brought to a targettemperature and/or pressure in a time period of between about 30 secondsand about 30 minutes.

In some embodiments, the reaction mixture may be brought to a targettemperature and/or pressure in a time period less than about 15 minutes,less than about 10 minutes, less than about 5 minutes, or less thanabout 2 minutes.

In certain embodiments, the reaction mixture may be brought to a targetpressure substantially instantaneously and brought to a targettemperature in less than about 20 minutes, less than about 10 minutes,or less than about 5 minutes. In other embodiments, the reaction mixturemay be brought to a target pressure substantially instantaneously andbrought to a target temperature in less than about two minutes. In otherembodiments, the reaction mixture may be brought to a target pressuresubstantially instantaneously and brought to a target temperature inbetween about 1 and about 2 minutes.

Additionally or alternatively, following completion of the retentiontime period the product mixture generated may be cooled to between about150° C. and about 200° C., between about 160° C. and about 200° C.,preferably between about 170° C. and about 190° C., and more preferablyabout 180° C., in a time period of less than about 10 minutes,preferably less than about 7 minutes, more preferably less than about 6minutes, preferably between about 4 and about 6 minutes, and morepreferably about 5 minutes. Following the initial cooling period, thetemperature may further reduced to ambient temperature with concurrentde-pressurisation by fast release into a cool aqueous medium (e.g.cooled water).

The processes of heating/pressurisation and cooling/de-pressurisationmay be facilitated by performing the methods of the present invention ina continuous flow system (see section below entitled “Continuous flow”).

Continuous flow

Bio-product generation from organic matter feedstocks (e.g.lignocellulosic matter) using the methods of the present invention maybe assisted by performing the methods under conditions of continuousflow.

Although the methods need not be performed under conditions ofcontinuous flow, doing so may provide a number of advantageous effects.For example, continuous flow may facilitate the acceleratedimplementation and/or removal of heat and/or pressure applied to theslurry. This may assist in achieving the desired rates of mass and heattransfer, heating/cooling and/or pressurisation/de-pressurisation.Continuous flow may also allow the retention time to be tightlycontrolled. Without limitation to a particular mode of action, it ispostulated that the increased speed of heating/cooling and/orpressurisation/de-pressurisation facilitated by continuous flowconditions along with the capacity to tightly regulate retention timeassists in preventing the occurrence of undesirable side-reactions (e.g.polymerisation) as the slurry heats/pressurises and/orcools/de-pressurises. Continuous flow is also believed to enhancereactions responsible for conversion of organic matter to biofuel byvirtue of generating mixing and shear forces believed to aid inemulsification which may be an important mechanism involved in thetransport and “storage” of the oils generated away from the reactivesurfaces of the feedstock as well as providing interface surface areafor so-called ‘on-water catalysis’.

Accordingly, in preferred embodiments the methods of the presentinvention are performed under conditions of continuous flow. As usedherein, the term “continuous flow” refers to a process wherein organicmatter feedstock mixed with a solvent in the form of a slurry (which mayfurther comprise any one or more of a solid substrate, an oil additiveand/or a catalyst additive) is subjected to:

(a) heating and pressurisation to a target temperature and pressure,

(b) treatment at target temperature(s) and pressure(s) for a definedtime period (i.e. the “retention time”), and

(c) cooling and de-pressurisation, while the slurry is maintained in astream of continuous movement along the length (or partial length) of agiven surface. It will be understood that “continuous flow” conditionsas contemplated herein are defined by a starting point of heating andpressurisation (i.e. (a) above) and by an end point of cooling andde-pressurisation (i.e. (c) above).

Continuous flow conditions as contemplated herein imply no particularlimitation regarding flow velocity of the slurry provided that it ismaintained in a stream of continuous movement.

Preferably, the minimum (volume-independent) flow velocity of the slurryalong a given surface exceeds the settling velocity of solid matterwithin the slurry (i.e. the terminal velocity at which a suspendedparticle having a density greater than the surrounding solution moves(by gravity) towards the bottom of the stream of slurry).

For example, the minimum flow velocity of the slurry may be above about0.01 cm/s, above about 0.05 cm/s, preferably above about 0.5 cm/s andmore preferably above about 1.5 cm/s. The upper flow velocity may beinfluenced by factors such as the volumetric flow rate and/or retentiontime. This in turn may be influenced by the components of a particularreactor apparatus utilised to maintain conditions of continuous flow.

Continuous flow conditions may be facilitated, for example, byperforming the methods of the invention in a suitable reactor apparatus.A suitable reactor apparatus will generally comprise heating/cooling,pressurising/de-pressuring and reaction components in which a continuousstream of slurry is maintained.

The use of a suitable flow velocity (under conditions of continuousflow) may be advantageous in preventing scale-formation along the lengthof a particular surface that the slurry moves along (e.g. vessel wallsof a reactor apparatus) and/or generating an effective mixing regime forefficient heat transfer into and within the slurry.

Bio-Products

The methods of the present invention may be used to producebio-product(s) from organic matter feedstocks (e.g. lignocellulosicmatter). The nature of the bio-product(s) may depend on a variety ofdifferent factors including, for example, the organic matter feedstocktreated, and/or the reaction conditions/reagents utilised in themethods.

In certain embodiments, the bio-product(s) may comprise one or morebiofuels (e.g. bio-oils, char products, gaseous products) and chemicalproducts (e.g. platform chemicals, organic acids, furanics, furfural,hydroxymethylfurfural, levoglucosan, sorbitol, cylitol, arabinitol,formaldehyde, acetaldehyde).

In general, bio-product(s) produced in accordance with the methods ofthe present invention comprise or consist of a bio-oil. The bio-oil maycomprise compounds including, but not limited to, any one or more ofalkanes, alkenes, aldehydes, carboxylic acids, carbohydrates, phenols,furfurals, alcohols, and ketones. The bio-oil may comprise compoundsincluding but not limited to aldehydes, carboxylic acids, carbohydrates,phenols, furfurals, alcohols, and ketones, resins and resin acids, andcompounds structurally related to resin acids, alkanes and alkenes,fatty acids and fatty acid esters, sterols and sterol-related compounds,furanic oligomers, cyclopentanones, and cyclohexanones, alkyl- andalkoxy-cyclopentanones, and cyclohexanones, cyclopenteneones, alkyl- andalkoxy-cyclopentenones, aromatic compounds including naphthalenes andalkyl- and alkoxy-substituted naphthalenes, cresols, alkyl- andalkoxy-phenols, alkyl- and alkoxy-catechols, alkyl- andalkoxy-dihydroxybezenes, alkyl- and alkoxy-hydroquinones, indenes andindene-derivatives.

The bio-oil may comprise multiple phases, including but not limited to awater-soluble aqueous phase which may comprise, compounds including, butnot limited to, any one or more of carbohydrates, aldehydes, carboxylicacids, carbohydrates, phenols, furfurals, alcohols, and ketones, resinsand resin acids, and compounds structurally related to resin acids,alkanes and alkenes, fatty acids and fatty acid esters, sterols andsterol-related compounds, furanic oligomers, cyclopentanones, andcyclohexanones, alkyl- and alkoxy-cyclopentanones, and cyclohexanones,cyclopenteneones, alkyl- and alkoxy-cyclopentenones, aromatic compoundsincluding naphthalenes and alkyl- and alkoxy-substituted naphthalenes,cresols, alkyl- and alkoxy-phenols, alkyl- and alkoxy-catechols, alkyl-and alkoxy-dihydroxyhezenes, alkyl- and alkoxy-hydroquinones, indenesand indene-derivatives; and a water-insoluble phase which may comprise,compounds including, but not limited to, any one or more of waxes,aldehydes, carboxylic acids, carbohydrates, phenols, furfurals,alcohols, and ketones, resins and resin acids, and compoundsstructurally related to resin acids, alkanes and alkenes, fatty acidsand fatty acid esters, sterols and sterol-related compounds, furanicoligomers, cyclopentanones, and cyclohexanones, alkyl- andalkoxy-cyclopentanones, and cyclohexanones, cyclopenteneones, alkyl- andalkoxy-cyclopentenones, aromatic compounds including naphthalenes andalkyl- and alkoxy-substituted naphthalenes, cresols, alkyl- andalkoxy-phenols, alkyl- and alkoxy-catechols, alkyl- and alkoxydihydroxybezenes, alkyl- and alkoxy-hydroquinones, indenes andindene-derivatives.

Other non-limiting examples of the bio-products include oil char (e.g.carbon char with bound oils), char, and gaseous product (e.g. methane,hydrogen, carbon monoxide and/or carbon dioxide, ethane, ethene,propene, propane).

In some embodiments, a biofuel may be produced from organic mattercomprising lignocellulosic matter. The biofuel may comprise a liquidphase comprising bio-oil.

Biofuels (e.g. bio-oils) produced in accordance with the methods of theinvention may comprise a number of advantageous features, non-limitingexamples of which include reduced oxygen content, increased hydrogencontent, increased energy content and increased stability. In addition,bio-oils produced by the methods of the invention may comprise a singleoil phase containing the liquefaction product. The product may beseparated from the oil phase using, for example, centrifugationeliminating the need to evaporate large amounts of water.

A bio-oil bio-product produced in accordance with the methods of theinvention may comprise an energy content of greater than about 25 MJ/kg,greater than about 30 MJ/kg, more preferably greater than about 32MJ/kg, more preferably greater than about 35 MJ/kg, still morepreferably greater than about 37 MJ/kg, 38 MJ/kg or 39 MJ/kg, and mostpreferably above about 41 MJ/kg. The bio-oil product may comprise lessthan about 15% wt db oxygen, preferably less than about 10% wt dboxygen, more preferably less than about 8% wt db oxygen and still morepreferably less than about 7% wt db oxygen, and preferably less thanabout 5% wt db oxygen. The bio-oil product may comprise greater thanabout 6% wt db hydrogen, preferably greater than about 7% wt dbhydrogen, more preferably greater than about 8% wt db hydrogen, andstill more preferably greater than about 9% wt db hydrogen. The molarhydrogen:carbon ratio of a bio-oil of the invention may be less thanabout 1.5, less than about 1.4, less than about 1.3, or less than about1.2.

A bio-oil produced in accordance with the methods of the invention maycomprise, for example, any one or more of the following classes ofcompounds: phenols, aromatic and aliphatic acids, ketones, aldehydes,hydrocarbons, alcohols, esters, ethers, furans, furfurals, terpenes,polycyclics, oligo- and polymers of each of the aforementioned classes,plant sterols, modified plant sterols, asphaltenes, pre-asphaltenes, andwaxes.

A char or oil char bio-product produced in accordance with the methodsof the invention may comprise an energy content of greater than about 20MJ/kg, preferably greater than about 25 MJ/kg, more preferably greaterthan about 30 MJ/kg, and still more preferably greater than about 31MJ/kg, 32 MJ/kg, 33 MJ/kg or 34 MJ/kg. The char or oil char product maycomprise less than about 20% wt db oxygen, preferably less than about15% wt db oxygen, more preferably less than about 10% wt db oxygen andstill more preferably less than about 9% wt db oxygen. The char or oilchar product may comprise greater than about 2% wt db hydrogen,preferably greater than about 3% wt db hydrogen, more preferably greaterthan about 4% wt db hydrogen, and still more preferably greater thanabout 5% wt db hydrogen. The molar hydrogen:carbon ratio of a char oroil char product of the invention may be less than about 1.0, less thanabout 0.9, less than about 0.8, less than about 0.7, or less than about0.6.

An oil char bio-product produced in accordance with the methods of theinvention may comprise, for example, any one or more of the followingclasses of compounds: phenols, aromatic and aliphatic acids, ketones,aldehydes, hydrocarbons, alcohols, esters, ethers, furans, furfurals,terpenes, polycyclics, oligo- and polymers of each of the aforementionedclasses, asphaltenes, pre-asphaltenes, and waxes.

A char bio-product (upgraded PCI equivalent coal) produced in accordancewith the methods of the invention may comprise, for example, a mixtureof amorphous and graphitic carbon with end groups partially oxygenated,giving rise to surface carboxy- and alkoxy groups as well as carbonyland esters.

Bio-products produced in accordance with the methods of the presentinvention may comprise one or more biofuels (e.g. bio-oils, charproducts, gaseous products) and chemical products (e.g. platformchemicals, organic acids, furanics, furfural, hydroxymethylfurfural,levoglucosan, sorbitol, cylitol, arabinitol, formaldehyde,acetaldehyde).

Bio-products produced in accordance with the methods of the presentinvention may be cleaned and/or separated into individual componentsusing standard techniques known in the art.

For example, solid and liquid phases of biofuel products (e.g. from theconversion of coal) may be filtered through a pressure filter press, orrotary vacuum drum filter in a first stage of solid and liquidseparation. The solid product obtained may include a high carbon charwith bound oils. In certain embodiments, the oil may be separated fromthe char, for example, by thermal distillation or by solvent extraction.The liquid product obtained may contain a low percentage of light oils,which may be concentrated and recovered though an is evaporator.

Bio-products produced in accordance with the methods of the presentinvention may be used in any number of applications. For example,biofuels may be blended with other fuels, including for example,ethanol, diesel and the like. Additionally or alternatively, thebiofuels may be upgraded into higher fuel products. Additionally oralternatively, the biofuels may be used directly, for example, aspetroleum products and the like.

It will be appreciated by persons skilled in the art that numerousvariations and/or modifications may be made to the invention as shown inthe specific embodiments without departing from the spirit or scope ofthe invention as broadly described. The present embodiments are,therefore, to be considered in all respects as illustrative and notrestrictive.

EXAMPLES

The invention will now be described with reference to specific examples,which should not be construed as in any way limiting

Example 1: Exemplary Conversion of Organic Matter to a Synthetic CrudeOil and Additional Chemical Products in the Presence of a SolidSubstrate: Comparison with Conversion in Absence of Solid Substrate (i)Slurry Preparation

Pre-ground feedstock (radiata pine biomass containing about 10-20 wt %water) was slurried with water in an agitated slurrying tank both withand without solid substrate. The solid substrate was either lignite(containing about 30-50% water) or activated carbon. For Run 10 theorganic matter was bana grass and the solid substrate was a mixture oflignite and iron oxide powder (haematite powder).

The particle size of the radiata pine organic matter was 0.15 mm-2mm.The particle size of the solid substrate was <2 mm.

The mixing proportions of the materials used in the series ofexperiments are given in Table 2 below.

TABLE 2 Examples of Slurry Compositions Organic Solid Aqueous Oil AddedOrganic Solid Aqueous Oil matter substrate solvent solvent Addedcatalyst % of Run Matter substrate solvent solvent % in % in % in % inCatalyst dry matter in No. type type type type slurry slurry slurryslurry type slurry 1 Radiata None Water — 12.2 — 87.8 — NaOH 14.2 pine 2Radiata None Water — 12.2 — 87.8 — NaOH 7.2 pine 3 Radiata None Water —15 — 85 — NaOH 8.0 pine 4 Radiata Lignite Water — 4 4 92 — NaOH 12 pine5 Radiata Lignite Water — 7 3 90 — NaOH 10 pine 6 Radiata ActivatedWater — 9 3 88 — NaOH 10 pine Carbon 7 Radiata Lignite Water — 7.8 4.787.5 — NaOH 9 pine 8 Radiata Lignite Water — 9.8 6 84.2 — NaOH 9 pine 9Radiata Lignite Water — 12 1.7 86.3 — NaOH 11 pine 10 Bana Lignite Water— 6 20 lignite 83.5 — — grass plus iron 0.5 oxide haematite (haematite)

An additional oil component was not added for this series ofexperiments. As the organic matter liquefies within a matter of secondsupon being raised to reaction temperature it is considered that there isan oil phase present within the reactor even in the runs where no addedoil solvent component is used, particularly for organic matterconcentrations in the slurry greater than 5 w/w.

(ii) Heating and Pressurisation

A high-pressure pump was fed by the slurrying tank to deliver the slurryto heating section at pressures ranges as shown in Table 3 below.Heating of the slurry can be performed in several ways, for example, bya counter or co-current heat exchange system and/or by immersion of theheating section in a hot fluidized bed. Alternatively, the slurry can beheated in a ballistic fashion by the intersection of the slurry in theheating section with an oil or water stream heated, for example, in therange of 400-720 degrees Celsius (see, for example, Australianprovisional patent application number 2010902938 entitled “Ballisticheating process”, the entire contents of which are incorporated hereinby reference). In all cases, the target slurry temperature was in therange of 250-350 degrees Celsius (centigrade) upon entering the reactor.In certain cases, one or more catalysts incorporated into the slurryprior to entry into the reactor.

In the particular experiments exemplified here the slurry was pre-heatedby means of a counterflow heat exchanger to about 150 C and then furtherheated by mixing with an incident stream of supercritical steam to about320-360 C before entering the reactor.

(iii) Conversion Reaction

The slurry was fed into the reactor (which can either have a vertical orhorizontal orientation) under conditions of continuous flow with thereacting slurry being kept at a constant temperature and pressure insidethe ranges as shown in Table 3 below. The residence time at the reactiontemperature was held to the range of 15-30 min. dependent on feedstockand catalyst/s applied. As the reaction is mildly endothermic (3-5 MJ/kgof product) only a small amount of trim heating was necessary.

This experimental observation means that little restriction exists tothe diameter of the reactor tube as it does not need to be heatedsubstantially; the thermal mass and lagging the reactor sufficed.Another major positive factor related to scaling the system and keepingthe reactor length to a minimum.

Catalyst was added as an aqueous solution between the heating step andthe reactor.

TABLE 3 Examples of Process Conditions Organic Solid Aqueous ReactorPressure Residence Pre-heater Run Matter substrate solvent temperatureRange time in temperature No. type type type range (C.) (Bar) Minutes(C.) 1 Radiata None Water 320-360 220-260 20-30 120-160 pine 2 RadiataNone Water 320-360 220-260 20-30 120-160 pine 3 Radiata None Water320-360 220-260 20-30 120-160 pine 4 Radiata Lignite Water 320-360220-260 20-30 120-160 pine 5 Radiata Lignite Water 320-360 220-260 20-30120-160 pine 6 Radiata Activated Water 320-360 220-260 20-30 120-160pine Carbon 7 Radiata Lignite Water 320-360 220-260 20-30 120-160 pine 8Radiata Lignite Water 320-360 220-260 20-30 120-160 pine 9 RadiataLignite Water 320-360 220-260 20-30 120-160 pine 10 Bana Lignite Water320-360 220-260 20-30 n/a Grass plus iron oxide

(iv) Cooling and Pressure Let-Down

At the end of the set residence time the product stream may optionallybe passed through a heat exchanger with an exit temperature in the rangeof 50-180 degrees Celsius (at which stage reaction rates slowsubstantially), this final set temperature being feedstock dependent.Alternatively and as exemplified here the pressure is let down toatmospheric pressure by one or more depressurisation steps. Specificallythe reacted mixture was depressurized by passing through a selectablecapillary system to either approximately 20 bar and then to atmosphericpressure or directly to atmospheric pressure. The exit of the capillarytube may be immersed in water or another liquid. The pressure let-downsystem was used to generate the back-pressure in the reactor and heatingsystem allowing a continuous flow reaction to be achieved at a constantpressure and temperature steady state. A suitable pressure let downsystem is described, for example, in United States of America patentpublication no. 2012-0227822 A1 entitled “Assembly for reducing slurrypressure in a slurry processing system”, the entire contents of whichare incorporated herein by reference.

(v) Results

In each case a water insoluble product separates from the aqueous phaseon cooling. The water insoluble product may be a liquid or a viscousmelt depending upon the ambient temperature and upon whether or not itcontains solid substrate and whether or not oil was used in the solventphase. Products containing solid substrate may be a glassy solidresembling pitch at ambient temperatures.

In each case the aqueous phase contains water soluble organic compounds.

It was observed that in the case where the no solid substrate was addedto the slurry feed, the pressure drop across the reactor, as measured bythe difference between a pressure gauge located before the reactor and apressure gauge located after the reactor but before the cooling ordepressurisation steps, increased substantially with run duration,possibly an indication of partial blockages developing inside thereactor. In contrast, where a solid substrate is added the pressure dropdeveloped over the reactor is negligible and does not increase overtime.

The pressure drops across the reactor recorded in a series ofexperiments with and without added solid substrate are shown in FIG. 2and FIG. 4.

It is a key feature of the present invention that it allows for thereaction of high concentrations of organic matter in large-scalecontinuous reactors without the need for the design of elaborate reactorprofiles at significantly higher cost.

For example it is possible that long straight tubular reactor withoutany profile changes could also overcome the development of a pressuredrop across the reactor, however such a reactor would need to be about18 metres long in order to achieve the same residence time as three 6metre reactors linked in series. Since a preferable configuration formany applications, in terms of reactor fabrication and arrangement tooccupy a minimum footprint area, is three vertically mounted 6 metretubes linked in series by narrow radius bends as opposed to an 18 metretube mounted in either horizontal or vertical configuration, the currentinvention leads to significant CapEx savings in the design of acommercial scale plant for the conversion of organic matter, especiallyin relation to lignocellulosic biomass.

(vi) Nature of Products from Process

Depending on the nature of the solid substrate employed, the solidsubstrate may be completely inert under reaction conditions and besubstantially unchanged, or it may act as a catalyst to assist in thetransformation of the organic matter to products, or it may partiallyreact and partially contribute to the formation of products of theprocess, or a combination of each may occur.

Without limitation to a particular mode of action substrates such asactivated carbon may, under the conditions described in this inventioncatalyse the conversion of organic matter to products containing lessoxygen by facilitating decarboxylation reactions. (See for exampleActivated Carbons for Hydrothermal Decarboxylation of Fatty Acids, JieFu, Fan Shi, L. T. Thompson, Jr., Xiuyang Lu, and Phillip E. Savage, ACSCatal., 2011, 1 (3), pp 227-231)

Where a solid substrate is employed it may be recovered from the processintimately mixed with water-insoluble fuel and chemical products.Alternatively and preferably the solid substrate is separated from thewater-insoluble fuel and chemical products before or immediately afterthe depressurisation step by means of a hydrocyclone, centrifuge,decanter, filter or other means of physical separation. In that case thesolid substrate is most preferably recycled into the process byslurrying with fresh organic matter being fed to the process.

Alternatively liquid products are partially separated from the solidsubstrate before or immediately after the depressurisation step by meansof a hydrocyclone, centrifuge, decanter, filter or other means ofphysical separation. In that case the liquid products are mostpreferably taken off as a product stream and the solid substrate mixedwith some liquid products is preferably recycled into the process byslurrying with fresh organic matter being fed to the process.

Alternatively fuel and chemical products are separated from solidsubstrate in a separate processing step for example by distillation orby extraction with a solvent. In that case the extracted fuel orchemical products that may be liquids or solids are taken off as aproduct stream and the residue, being the solid substrate is preferablyrecycled into the process by slurrying with fresh organic matter beingfed to the process.

In all cases solid substrate that is excess to requirements forrecycling into the process constitutes an additional product, forinstance a solid fuel, a coking or PCI coal, a precursor to activatedcarbon.

Certain properties of the water-insoluble products from the runsexemplified are shown in Tables 4 and 5.

In the case of the examples containing a solid substrate the propertieslabelled “Solid Substrate . . . Initial” are those corresponding to thesolid substrate as mixed into the reaction mixture or slurry beforepassing through the reactor. The properties labelled “Mixed SolidSubstrate & Oil Product” are those of the mixture of solid substrate andwater-insoluble product oil after passing through the reaction andcooling and depressurization steps. The properties labelled “Separatedoil Product” are those properties of the water-insoluble oil productafter separation from the solid substrate. The properties labelled‘Recovered Solid substrate/solid product” are the properties of theresidual solid material after removal of the oil product. This materialcan be recycled after, if necessary, crushing or milling to a suitableparticle size, as solid substrate to be combined with new organic matterentering the process.

Without limitation, the means used to separate the oil products from thesolid substrate in these example were: solvent extraction with acetoneor tetrahydofuran solvents; vacuum distillation or vacuum sublimation;distillation including partially-pyrolitic distillation under a flow ofinert gas or vapour, for example steam and/or nitrogen or argon.

The thermal separation of the products from the solid substrate isexemplified by thermogravimetric analysis (TGA) of the products undernitrogen atmosphere. FIG. 3 shows the weight loss versus temperature forsamples of Mixed Solid Substrate & Oil Product from runs 5 (twosamples), 6, and 7. The data illustrate that up to 50% by mass of thesamples in question may be volatilized up to temperatures of 400° C.

TABLE 4 Properties of the water-insoluble products from the runsexemplified. Mixed Solid Solid Organic Substrate Substrate SeparatedRecovered matter GCV & Oil oil Solid GCV initial Product Productsubstrate/solid Organic Solid (MJ/kg (MJ/kg GCV GCV product GCV RunMatter substrate dry dry (MJ/kg dry (MJ/kg (MJ/kg No. type type basis)basis) basis) dry basis) dry basis) 1 Radiata None 21 n/a n/a 34 pine 2Radiata None 21 n/a n/a 34 pine 3 Radiata None 21 n/a n/a 34 pine 4Radiata Lignite 21 25 — 37 27 pine 5 Radiata Lignite 21 25 30.6 36 31.7pine 6 Radiata Activated 21 30.5 33.4 33.5 29.3 pine Carbon 7 RadiataLignite 21 25 — 36.3 pine 8 Radiata Lignite 21 25 — — pine 9 RadiataLignite 21 25 — — pine 10 Bana Lignite 18.5 25 28.3 38.3 26.10 Grassplus iron oxide

TABLE 5 Examples of Water-insoluble Product Properties Solid Ultimateanalysis of Separated Ultimate analysis of recovered Run Organicsubstrate Oil product dry basis substrate/solid product dry basis No.Matter type type % C % H % N % S % Ash % O % C % H % N % S % Ash % O 1Radiata pine None 79.8 6.62 1.5  12 2 Radiata pine None 78.2 7.01 0.4 14.1 3 Radiata pine None 78 7.02 0.18 14.7 4 Radiata pine Lignite 80.18.4  0.18 0.29 10.3 72.96 4.30 0.40 5.74 16.40 5 Radiata pine Lignite 6Radiata pine Activated 75.8 7.33 0.58 0.18 16.1 73.23 3.54 0.91 7.1215.20 Carbon 7 Radiata pine Lignite 8 Radiata pine Lignite 9 Radiatapine Lignite 10 Bana Grass Lignite plus 83.47 8.90 0.28 0.17 0.02 7.1674.5  3.90 0.85 0.26 7.2  13.3  iron oxide

(vii) Composition of Products

The water-soluble and water-insoluble products from the reaction arecomplex mixtures of organic compounds. Listed in Table 6 below are anumber of components identified in the water-soluble and water-insolublephases of the products, where the organic matter comprised radiata pine.Most of the components are common to both water-soluble andwater-insoluble phases.

TABLE 6 Components identified in the water-soluble and water-insolublephases of the products Compound 2-methyl-2-cyclopentene-1-one3-methyl-2-cyclopentene-1-one 3,4-dimethyl-2-cyclopentene-1-one2,3-dimethyl-2-cyclopentene-1-one 2,3,4-trimethyl-2-cyclopentene-1-one3-ethyl-2-cyclopentene-1-one m-Guaiacol (Mequinol) 3-Methylguaiacol4-Methylguaiacol 4-Ethylguaiacol 4-Propylguaiacol (Dihydroeugenol)4-Vinylguaiacol Eugenol (4-Allylguaiacol) Isoeugenol(4-Propenylguaiacol) Vanillin (4-hydroxy-3-methoxy-benzaldehyde)Homovanillyl alcohol (4-hydroxy-3-methoxy- phenylethanol) Homovanillicacid (4-Hydroxy-3-methoxy- phenylacetic acid) Phenol o-Cresol m-Cresolp-Cresol 2-Ethylphenol 3-Ethylphenol 4-Ethylphenol 2,3-dimethyl-phenol2,3,6-trimethyl-phenol 4-Propylphenol Pyrocatechol Hydroquinone3-Methyl-catechol 4-Methyl-catechol 2-Methyl-Hydroquinone2,3-Dimethyl-Hydroquinone 2,5-Dimethyl-Hydroquinone2,6-Dimethyl-Hydroquinone 4-Ethyl-catechol 4-Ethyl-1,3-Benzenediol4-propyl-1,3-Benzenediol 1-Butanol 4-Hydroxy-acetophenone4-Hydroxy-2-methylacetophenone 4-Hydroxy-1-indanone Abietic acid/Pimaricacid Cyclopentanone 3-Methyl-1-hexene 3-Methylcyclopentanone 2-Octene3-Ethyl-cyclopentanone Giberrelic acid 2,3-dihydro-1H-Inden-1-one2,3-dihydro-2-methyl-1H-Inden-1-one 2,3-dihydro-1H-Inden-5-ol1-Methylindan-2-one 7-Methylindan-1-one Oleic acid 9-Octadecenoic acid(Z)-, methyl ester 1,2,3,4-tetrahydro-5,7-dimethyl-Naphthalene4-methyl-1-Naphthalenol Androstan derivatives2-Isopropyl-10-methylphenanthrene Tetracosane C24H50 TetratriacontaneC34H70 Hexatriacontane C36H74 Methanol Ethanol Acetone

(viii) Discussion

It is clear from the preceding examples that the addition of a solidsubstrate inhibits the build-up over time of a pressure differenceacross a tube-like reactor under continuous flow conditions. The solidsubstrate does not detract from the calorific value of the bio-productsobtained, but in fact provides significant enhancement. Oil bio-productsmay be separated from the substrate by a variety of physical methods.The residual substrate may be recycled into the process or if notrequired for that purpose it represents a solid bio-product.

Example 2: Further Exemplary Conversion of Organic Matter to a SyntheticCrude Oil and Additional Chemical Products in the Presence of a SolidSubstrate (i) Slurry Preparation

Pre-ground feedstock (radiata pine biomass containing about 10-20 wt %water) was slurried with water in an agitated slurrying tank with solidsubstrate. The solid substrate was either lignite or activated carbon.

The mixing proportions of the materials used in the series ofexperiments are given in Table 7 below.

(ii) Heating and Pressurisation

Samples were pre-heated and a high-pressure pump was fed by theslurrying tank to deliver the slurry to the main part of the reactor.Heating of the slurry can be performed in several ways, for example, bya counter or co-current heat exchange system and/or by immersion of theheating section in a hot fluidized bed. Alternatively, the slurry can beheated in a ballistic fashion by the intersection of the slurry in theheating section with an oil or water stream (e.g. supercritical steam)(see, for example, United States of America patent publication no.2013-0205652 A1 entitled “Ballistic heating process”, the entirecontents of which are incorporated herein by reference).

In all cases, the target slurry temperature was in the range of 250-350°C. upon entering the reactor. In certain cases, one or more catalystsincorporated into the slurry prior to entry into the reactor. In theparticular experiments exemplified here the slurry was pre-heated bymeans of a counterflow heat exchanger to about 150° C. and then furtherheated by mixing with an incident stream of supercritical steam to about320-360° C. before entering the reactor.

(iii) Conversion Reaction

The slurry was fed into the reactor (which can either have a vertical orhorizontal orientation) under conditions of continuous flow with thereacting slurry being kept at a constant temperature and pressure insidethe ranges as shown in Table 8 below. The residence time at the reactionconditions is also shown in Table 8.

Catalyst was added as an aqueous solution after contact with thesupercritical steam prior to the heated and pressurised slurry enteringthe reactor.

(iv) Cooling and Pressure Let-Down

At the end of the set residence time the product stream may optionallybe passed through a heat exchanger with an exit temperature in the rangeof 50-180 degrees Celsius (at which stage reaction rates slowsubstantially), this final set temperature being feedstock dependent.Alternatively and as exemplified here the pressure is let down toatmospheric pressure by one or more depressurisation steps. Specificallythe reacted mixture was depressurized by passing through a selectablecapillary system to either approximately 20 bar and then to atmosphericpressure or directly to atmospheric pressure. The exit of the capillarytube may be immersed in water or another liquid. The pressure let-downsystem was used to generate the back-pressure in the reactor and heatingsystem allowing a continuous flow reaction to be achieved at a constantpressure and temperature steady state. A suitable pressure let downsystem is described, for example, in United States of America patentpublication no. 2012-0227822 A1 entitled “Assembly for reducing slurrypressure in a slurry processing system”, the entire contents of whichare incorporated herein by reference.

(v) Product Analysis

Certain properties of the water-insoluble products from the runsexemplified are shown in Tables 9 and 10. Without limitation, the meansused to separate the oil products from the solid substrate in theseexamples were: solvent extraction with acetone or tetrahydrofuransolvents; vacuum distillation or vacuum sublimation; distillationincluding partially-pyrolitic distillation under a flow of inert gas orvapour (e.g. steam and/or nitrogen or argon).

TABLE 7 Slurry Compositions (A-J) Prepared for Processing PercentageAqueous Run of Total Feedstock Solid Substrate Added Catalyst SolventNo. Solids in Slurry Type/Percentage Type/Percentage Type/AmountParticle size Type A ≈10 wt % dry basis Radiata pine Lignite NaOHRadiata pine Water in slurry ≈7 wt % of total (coal powder) ≈10% ratio≈500 ⊏M dry solids in ≈3 wt % of total (0.1:1) Lignite slurry dry solidsin slurry of total solids in ≈<1 mm, sieved slurry B ≈15 wt % dry basisRadiata pine Carbon (activated) NaOH Radiata pine Water in slurry ≈9 wt% of total ≈6 wt % of total ≈15% ratio ≈500 ⊏M dry solids in dry solidsin slurry (0.15:1) Lignite slurry) of total solids in ≈<1 mm, sievedslurry C ≈15 wt % dry basis Radiata pine Lignite NaOH Radiata pine Waterin slurry ≈8.5 wt % of total ≈7.5 wt % of total ≈15% ratio ≈500 ⊏M drysolids in dry solids in slurry (0.15:1) Lignite slurry of total solidsin ≈<1 mm, sieved slurry D ≈14 wt % dry basis Radiata pine Lignite NaOHRadiata pine Water in slurry ≈12 wt % of total ≈1.7 wt % of total ≈14%ratio ≈500 ⊏M dry solids in dry solids in slurry (0.14:1) Lignite slurryof total solids in ≈<1 mm, sieved slurry E ≈14 wt % dry basis Radiatapine Lignite NaOH Radiata pine Water in slurry ≈13 wt % of total ≈0.9 wt% of total ≈14% ratio ≈500 ⊏M dry solids in dry solids in slurry(0.14:1) Lignite slurry of total solids in ≈<1 mm, sieved slurry F ≈15wt % dry basis Radiata pine Lignite NaOH Radiata pine Water in slurry≈9.8 wt % of total ≈6 wt % of total ≈15% ratio ≈500 ⊏M dry solids in drysolids in slurry (0.15:1) Lignite slurry of total solids in ≈<1 mm,sieved slurry G ≈14 wt % dry basis Radiata pine Lignite NaOH Radiatapine Water in slurry ≈10 wt % of total ≈3 wt % of total ≈14% ratio ≈500⊏M dry solids in dry solids in slurry (0.14:1) Lignite slurry of totalsolids in ≈<1 mm, sieved slurry H ≈9 wt % dry basis Radiata pine LigniteNaOH Radiata pine Water in slurry ≈9 wt % of total ≈1.6 wt % of total≈9% ratio ≈500 ⊏M dry solids in dry solids in slurry (0.09:1) Ligniteslurry of total solids in ≈<1 mm, sieved slurry I ≈14 wt % dry basisRadiata pine Lignite NaOH Radiata pine Water in slurry ≈12 wt % of total≈2 wt % of total dry ≈14% ratio ≈500 ⊏M dry solids in solids in slurry(0.14:1) Lignite slurry of total solids in ≈<1 mm, sieved slurry J ≈14wt % dry basis Radiata pine Lignite NaOH Radiata pine Water in slurry≈12 wt % in ≈2 wt % of total dry ≈14% ratio ≈500 ⊏M slurry) solids inslurry) (0.14:1) Lignite of total solids in ≈<1 mm, sieved slurry NOTES:≈approximately

TABLE 8 Conditions for processing slurry compositions (A-J) ReactorReactor Preheater temperature pressure Residence Temperature Run No.Range (° C.) range (Bar) time (mins) (° C.) A 280-340 ≈230-240 ≈25 mins≈170-200 B 293-340 ≈230-240 ≈25 mins ≈170-200 C 284-338 ≈229-241 ≈25mins ≈170-200 D 286-335 ≈219-243 ≈25 mins ≈170-200 E 280-350 ≈220-240≈25 mins ≈170-200 F 275-344 ≈215-245 ≈25 mins ≈170-200 G 275-329≈218-242 ≈25 mins ≈170-200 H 339-370 ≈208-238 ≈25 mins ≈170-200 I337-373 ≈220-250 ≈25 mins ≈170-200 J 340-360 ≈220-250 ≈25 mins ≈170-200NOTES: ≈approximately

TABLE 9 Properties of the water-insoluble products from processingslurry compositions (A, C-F) Mixed Solid Recovered Solid Substrate &Separated oil substrate/solid Oil Product GCV Product GCV product GCVRun No. (MJ/kg dry basis) (MJ/kg dry basis) (MJ/kg dry basis) A 31.6 33.2  31.8  C 27.14 33.46 29.35 D 35.75 Separated oil Product—GCVcalculated from elemental analysis(MJ/kg dry basis) E 36.09 F 37.26

TABLE 10 Properties of the water-insoluble products from processingslurry compositions (C-F) Ultimate analysis of Separated Ultimateanalysis of recovered Oil product dry basis substrate/solid product drybasis Molar Molar Run H/C H/C No. % C % H % N % Ash % O Ratio % C % H %N % Ash % O Ratio C 75.79 7.33 0.58 0.18 16.12 1.15 73.23 3.54 0.91 7.1215.2 0.58 D 80.45 8.49 0.19 0.15 10.72 1.26 E 78.29 8.41 0.08 0.1 13.131.28 F 80.81 8.32 0.18 10.7 1.23 Oxygen by difference % O = 100 − % C-%H-% N-% Ash

1.-20. (canceled)
 21. A method of inhibiting a substantial pressuregradient in a continuous or a semi-continuous flow reactor for theproduction of a product mixture, comprising: providing a reactionmixture comprising the organic matter feedstock and a solid substrate tothe continuous or a semi-continuous flow reactor, the solid substratethereby inhibiting a substantial pressure gradient of the reactionmixture while in the continuous or a semi-continuous flow reactor. 22.The method of claim 21 wherein the continuous or a semi-continuous flowreactor is a reactor vessel comprising reactor vessel walls and whereininhibiting a substantial pressure gradient in the continuous or asemi-continuous flow reactor results from the solid substrate causingsubstantial avoidance of at least one of char and scale accumulation onthe reactor vessel walls.
 23. The method of claim 21 wherein thecontinuous or a semi-continuous flow reactor is a reactor vesselcomprising reactor vessel walls, and avoidance of at least one of charand scale accumulation on the reactor vessel walls provides for theability of separation of components of the product mixture, a componentof the product mixture comprising organic matter feedstock that becomescharred in the continuous or a semi-continuous flow reactor.
 24. Themethod of claim 23 wherein charred organic matter feedstock is acomponent of the product mixture and is separated from the productmixture by thermally treating the product mixture to generate thecarbon-rich char.
 25. The method of claim 24 wherein thermally treatingthe product mixture is in the substantial absence of oxygen.
 26. Themethod of claim 23 wherein the method comprises producing a carbon-richchar from charred organic matter retrieved during the separation. 27.The method of claim 21 wherein the reaction mixture comprises a solventand the solid substrate comprises between 5% and 15% of the totalcombined mass of the solid substrate and organic matter feedstock.
 28. Amethod for the production of a product mixture utilising a continuous ora semi-continuous reactor vessel having reactor vessel walls,comprising: providing a reaction mixture comprising organic matterfeedstock and a solid substrate, the solid substrate thereby providingsubstantial avoidance of at least one of char and scale accumulation onthe reactor vessel walls.
 29. The method of claim 28 wherein thereaction mixture comprises a solvent and the solid substrate sequestersat least one of organic and/or inorganic matter that de-solubiliseswithin the reaction mixture while in the continuous or a semi-continuousflow reactor.
 30. The method of claim 28 wherein charred organic matteris a component of the product mixture and is separated from the productmixture.
 31. The method of claim 30 wherein charred organic matter is acomponent of the product mixture and is separated from the productmixture by thermally treating the product mixture to generate thecarbon-rich char.
 32. The method of claim 31 wherein thermally treatingthe product mixture is in the substantial absence of oxygen.
 33. Themethod of claim 28 wherein substantial avoidance of at least one of charand scale accumulation on the reactor vessel walls inhibits asubstantial pressure gradient in the continuous or a semi-continuousflow reactor.
 34. The method of claim 30 wherein the method comprisesproducing a carbon-rich char from charred organic matter separated fromthe product mixture.
 35. The method of claim 28 wherein the solidsubstrate comprises between 5% and 15% of the total combined mass of thesolid substrate and organic matter feedstock.
 36. A method for producinga carbon-rich char from organic matter feedstock, the method comprising:providing a reaction mixture comprising the organic matter feedstock anda solid substrate; treating the reaction mixture in a reactor vessel ata reaction temperature and pressure suitable for conversion of all or aportion of the organic matter feedstock into a product mixture; anddepressurising and cooling the product mixture; wherein the solidsubstrate is solid or substantially solid at the reaction temperatureand pressure and sequesters organic and/or inorganic matter thatde-solubilises within the reaction mixture or the product mixture;thermally treating the product mixture to generate the carbon-rich char;and separating the carbon-rich char from the product mixture.
 37. Themethod of claim 36 wherein in the reactor vessel comprises reactorvessel walls and the solid substrate provides substantial avoidance ofat least one of char and scale accumulation on the reactor vessel walls.38. The method of claim 36 wherein the solid substrate inhibitsformation of a substantial pressure gradient within the reaction vesselduring conversion of all or a portion of the organic matter feedstockinto a product mixture.
 39. The method of claim 36 wherein the reactionmixture comprises a solvent and the solid substrate comprises between 5%and 15% of the total combined mass of the solid substrate and organicmatter feedstock.
 40. The method of claim 36 wherein thermally treatingthe product mixture is in the substantial absence of oxygen.